Methods of refining and producing isomerized fatty acid esters and fatty acids from natural oil feedstocks

ABSTRACT

Methods are provided for refining natural oil feedstocks and producing isomerized esters and acids. The methods comprise providing a C4-C18 unsaturated fatty ester or acid, and isomerizing the fatty acid ester or acid in the presence of heat or an isomerization catalyst to form an isomerized fatty ester or acid. In some embodiments, the methods comprise forming a dibasic ester or dibasic acid prior to the isomerizing step. In certain embodiments, the methods further comprise hydrolyzing the dibasic ester to form a dibasic acid. In certain embodiments, the olefin is formed by reacting the feedstock in the presence of a metathesis catalyst under conditions sufficient to form a metathesized product comprising olefins and esters, separating the olefins from the esters in the metathesized product, and transesterifying the esters in the presence of an alcohol to form a transesterified product having unsaturated esters.

CROSS REFERENCE TO RELATED APPLICATIONS

This application is a continuation-in-part application of U.S. patentapplication Ser. No. 13/647,825, filed Oct. 9, 2012, and U.S. patentapplication Ser. No. 12/901,829, filed Oct. 11, 2010, which claims thebenefit of U.S. Provisional Patent Application No. 61/250,743, filedOct. 12, 2009, the disclosures of which are incorporated herein byreference.

GOVERNMENT RIGHTS

This invention was made with Government support under grant no.DE-EE0002872/001 awarded by the Department of Energy. The U.S.Government has certain rights in this invention.

BACKGROUND

Metathesis is a catalytic reaction generally known in the art thatinvolves the interchange of alkylidene units among compounds containingone or more double bonds (e.g., olefinic compounds) via the formationand cleavage of the carbon-carbon double bonds. Metathesis may occurbetween two like molecules (often referred to as self-metathesis) and/orit may occur between two different molecules (often referred to ascross-metathesis). Self-metathesis may be represented schematically asshown in Equation I.R¹—CH═CH—R²+R¹—CH═CH—R²

R¹—CH═CH—R¹+R²—CH═CH—R²  (I)

wherein R¹ and R² are organic groups.

Cross-metathesis may be represented schematically as shown in EquationII.R¹—CH═CH—R²+R³—CH═CH—R⁴

R¹—CH═CH—R³+R¹—CH═CH—R⁴+R²—CH═CH—R³+R²—CH═CH—R⁴+R¹—CH═CH—R¹+R²—CH═CH—R²+R³—CH═CH—R³+R⁴—CH═CH—R⁴  (II)

wherein R¹, R², R³, and R⁴ are organic groups.

In recent years, there has been an increased demand for environmentallyfriendly techniques for manufacturing materials typically derived frompetroleum sources. For example, researchers have been studying thefeasibility of manufacturing biofuels, waxes, plastics, and the like,using natural oil feedstocks, such as vegetable and seed-based oils. Inone non-limiting example, metathesis catalysts are used to manufacturecandle wax, as described in PCT/US2006/000822, which is hereinincorporated by reference in its entirety. Metathesis reactionsinvolving natural oil feedstocks offer promising solutions for today andfor the future.

Natural oil feedstocks of interest include non-limiting examples such asnatural oils (e.g., vegetable oils, fish oil, animal fats) andderivatives of natural oils, such as fatty acids and fatty acid alkyl(e.g., methyl) esters. These feedstocks may be converted intoindustrially useful chemicals (e.g., waxes, plastics, cosmetics,biofuels, etc.) by any number of different metathesis reactions.Significant reaction classes include, as non-limiting examples,self-metathesis, cross-metathesis with olefins, and ring-openingmetathesis reactions. Representative non-limiting examples of usefulmetathesis catalysts are provided below. Metathesis catalysts can beexpensive and, therefore, it is desirable to improve the efficiency ofthe metathesis catalyst.

In recent years, there has been an increased demand for petroleum-basedtransportation fuels. Concerns exist that the world's petroleumproduction may not be able to keep up with demand. Additionally, theincreased demand for petroleum-based fuels has resulted in a higherproduction of greenhouse gases. In particular, the airline industryaccounts for greater than 10% of the greenhouse gases within the UnitedStates. Due to the increased demand for fuel and increased production ofgreenhouse gases, there is a need to explore methods of producingenvironmentally-friendly, alternative fuel sources. In particular, thereis a need to explore methods of producing environmentally friendly fuelcompositions and specialty chemicals from a natural feedstock.

SUMMARY

Methods are disclosed for refining a natural oil feedstock through ametathesis reaction of the natural oil feedstock in the presence of ametathesis catalyst.

In one embodiment, a method is provided for making an isomerized esteror acid. The method comprises providing a C4-C22 unsaturated fatty acidor unsaturated fatty acid ester. The method further comprisesisomerizing the unsaturated fatty acid or the unsaturated fatty acidester in the presence of heat or an isomerization catalyst to form anisomerized acid or isomerized acid ester. In some embodiments, theunsaturated fatty acid ester is derived from transesterifying a naturaloil feedstock in the presence of an alcohol to form the unsaturatedfatty acid ester. In other embodiments, the method may further comprise,prior to the isomerizing step, hydrolyzing the unsaturated fatty acidester to form the unsaturated fatty acid.

In some embodiments, the unsaturated fatty acid or the unsaturated fattyacid ester is selected from the group consisting of: pentenoic acidesters, hexenoic acid esters, heptenoic acid esters, octenoic acidesters, nonenoic acid esters, decenoic acid esters, undecenoic acidesters, dodecenoic acid esters, tridecenoic acid esters, tetradecenoicacid esters, pentadecenoic acid esters, hexadecenoic acid esters,heptadecenoic acid esters, octadecenoic acid esters, acids thereof, andmixtures thereof. In some embodiments, the melting point of theisomerized acid or the isomerized acid ester is reduced by at least 10°C. in comparison to the unsaturated fatty acid or the unsaturated fattyacid ester. In other embodiments, the solubility of the isomerized acidor the isomerized acid ester at ambient temperature is at least 10%higher in comparison to the solubility of the unsaturated fatty acid orthe unsaturated fatty acid ester.

In certain embodiments, the isomerizing step is conducted by heating areactor containing the dibasic ester or dibasic acid to a temperaturegreater than 100° C. In some embodiments, the isomerization catalyst is(PCy₃)₂(Cl)(H)Ru(CO). In other embodiments, the isomerization catalystis a sulfonated tetrafluoroethylene polymer.

In certain embodiments, the unsaturated fatty acid or unsaturated fattyacid ester comprises a terminal olefin ester having the followingstructure:

wherein X is a C₃-C₁₈ saturated or unsaturated alkyl chain, and R is analkyl group or hydrogen. R may be methyl. In certain embodiments, themethod further comprises, prior to the isomerizing step, providing aninternal olefin and reacting the terminal olefin ester with the internalolefin in the presence of a metathesis catalyst to form a dibasic esteror dibasic acid, wherein, in the subsequent isomerizing step, anisomerized dibasic ester or isomerized dibasic acid is formed. In someembodiments, the method further comprises hydrogenating the isomerizeddibasic ester or isomerized dibasic acid. In other embodiments, themethod further comprises reacting the isomerized dibasic ester orisomerized dibasic acid with itself or a low-molecular-weight olefin inthe presence of metathesis catalyst to form a metathesized dibasic esteror metathesized dibasic acid. In yet other embodiments, the terminalolefin ester is selected from the group consisting of: 4-pentenoic acidester, 5-hexenoic acid ester, 6-heptenoic acid ester, 7-octenoic acidester, 8-nonenoic acid ester, 9-decenoic acid ester, 10-undecenoic acidester, 11-dodecenoic acid ester, 12-tridecenoic acid ester,13-tetradecenoic acid ester, 14-pentadecenoic acid ester,15-hexadecenoic acid ester, 16-heptadecenoic acid ester, 17-octadecenoicacid ester, acids thereof, and mixtures thereof. In one embodiment, theterminal olefin is 9-decenoic acid ester. In yet other embodiments, theinternal olefin ester is selected from the group consisting of:pentenoic acid esters, hexenoic acid esters, heptenoic acid esters,octenoic acid esters, nonenoic acid esters, decenoic acid esters,undecenoic acid esters, dodecenoic acid esters, tridecenoic acid esters,tetradecenoic acid esters, pentadecenoic acid esters, hexadecenoic acidesters, heptadecenoic acid esters, octadecenoic acid esters, acidsthereof, and mixtures thereof. In one particular embodiment, theinternal olefin is 9-dodecenoic acid ester. In certain embodiments, themethod further comprises hydrolyzing the isomerized dibasic ester toform an isomerized dibasic acid.

In another embodiment, a method of refining a natural oil comprisesproviding a feedstock comprising a natural oil and reacting thefeedstock in a metathesis reactor in the presence of a first metathesiscatalyst to form a metathesized product comprising olefins and esters.The method further comprises separating the olefins in the metathesizedproduct from the esters in the metathesized product. The method furthercomprises transesterifying the esters in the presence of an alcohol toform a transesterified product comprising a terminal olefin ester havingthe following structure:

wherein X is a C₃-C₁₈ saturated or unsaturated alkyl chain, and R is analkyl group (e.g., methyl). The method further comprises isomerizing theterminal olefin ester in the presence of heat or an isomerizationcatalyst to form an isomerized fatty acid ester.

In certain embodiments, the isomerizing step is conducted by heating areactor containing the terminal olefin ester to a temperature greaterthan 100° C. In other embodiments, the isomerization catalyst is(PCy₃)₂(Cl)(H)Ru(CO). In some embodiments, the isomerization catalyst isa sulfonated tetrafluoroethylene polymer.

In some embodiments, the method further comprises hydrogenating theisomerized fatty acid ester. In certain embodiments, the terminal olefinester is selected from the group consisting of: 4-pentenoic acid ester,5-hexenoic acid ester, 6-heptenoic acid ester, 7-octenoic acid ester,8-nonenoic acid ester, 9-decenoic acid ester, 10-undecenoic acid ester,11-dodecenoic acid ester, 12-tridecenoic acid ester, 13-tetradecenoicacid ester, 14-pentadecenoic acid ester, 15-hexadecenoic acid ester,16-heptadecenoic acid ester, 17-octadecenoic acid ester, and mixturesthereof. In one particular embodiment, the terminal olefin ester is9-decenoic acid ester.

In other embodiments, the method further comprises hydrolyzing theterminal olefin ester prior to the isomerizing step to form a terminalolefin acid, wherein the isomerizing step forms an isomerized fattyacid.

In certain embodiments, the method further comprises, prior to theisomerizing step, providing an internal olefin and reacting the terminalolefin with the internal olefin in the presence of a second metathesiscatalyst to form a dibasic ester, wherein, in the subsequent isomerizingstep, the isomerized fatty acid ester is an isomerized dibasic ester.The internal olefin ester may be selected from the group consisting of:pentenoic acid esters, hexenoic acid esters, heptenoic acid esters,octenoic acid esters, nonenoic acid esters, decenoic acid esters,undecenoic acid esters, dodecenoic acid esters, tridecenoic acid esters,tetradecenoic acid esters, pentadecenoic acid esters, hexadecenoic acidesters, heptadecenoic acid esters, octadecenoic acid esters, andmixtures thereof. In one embodiment, the internal olefin ester is9-dodecenoic acid ester. In some embodiments, internal olefin ester isformed by reacting a portion of the terminal olefin ester with alow-molecular-weight internal olefin in the presence of a thirdmetathesis catalyst. The low-molecular-weight internal olefin may beselected from the group consisting of: 2-butene, 2-pentene, 2-hexene,3-hexene, 2-heptene, 3-heptene, 2-octene, 3-octene, 2-nonene, 3-nonene,and mixtures thereof.

In some embodiments, the method further comprises hydrogenating theisomerized dibasic ester. In other embodiments, the method furthercomprises hydrolyzing the dibasic ester.

In another embodiment, the method comprises reacting a feedstockcomprising a natural oil in the presence of a metathesis catalyst underconditions sufficient to form a metathesized product, wherein themetathesized product comprises olefins and esters. The method furthercomprises separating the olefins in the metathesized product from theesters in the metathesized product. The method further comprisestransesterifying the esters in the presence of an alcohol to form atransesterified product comprising 9-decenoic acid ester. The methodfurther comprises reacting the 9-decenoic acid ester with 9-dodecenoicacid ester in the presence of a second metathesis catalyst to form9-octadecene dioic acid ester. The method further comprises heating the9-octadecene dioic acid ester in a reactor at a temperature greater than100° C. to form an isomerized dibasic ester. In some embodiments, anisomerization catalyst is also used in the isomerizing step. In certainembodiments, the isomerization catalyst is (PCy₃)₂(Cl)(H)Ru(CO). Inother embodiments, the isomerization catalyst is a sulfonatedtetrafluoroethylene polymer.

In certain embodiments, the 9-dodecenoic acid ester is formed byreacting a portion of the 9-decenoic acid ester with alow-molecular-weight internal olefin in the presence of a thirdmetathesis catalyst. In one embodiment, the low-molecular-weightinternal olefin is 3-hexene.

In some embodiments, the isomerized dibasic ester is hydrolyzed to forman isomerized dibasic acid. In other embodiments, the isomerized dibasicester is self-metathesized to form a metathesized dibasic ester.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a schematic diagram of one embodiment of a process to producea fuel composition and a transesterified product from a natural oil.

FIG. 2 is a chart showing the weight % distribution of 9-DAME & 9-DDAMEas a function of cross-metathesis reaction time (hr).

FIG. 3 is a product distribution chart for 24 hour isomerizationreactions of 9-DAME with varying amounts isomerization catalyst (3 wt %and 5 wt %).

FIG. 4 is a product distribution chart for 9-DAME isomerizationreactions at varying reaction times (6 hr and 24 hr).

FIG. 5 is a product distribution chart for a 9-DDAME isomerizationreactions at varying reaction times (6 hr and 24 hr).

FIG. 6 is a product distribution chart for a 9-DAME isomerizationreaction.

FIG. 7 is a product distribution chart for a 9-DDAME isomerizationreaction.

DETAILED DESCRIPTION

As used herein, the singular forms “a,” “an,” and “the” include pluralreferents unless the context clearly dictates otherwise. For example,reference to “a substituent” encompasses a single substituent as well astwo or more substituents, and the like.

As used herein, the terms “for example,” “for instance,” “such as,” or“including” are meant to introduce examples that further clarify moregeneral subject matter. Unless otherwise specified, these examples areprovided only as an aid for understanding the applications illustratedin the present disclosure, and are not meant to be limiting in anyfashion.

As used herein, the following terms have the following meanings unlessexpressly stated to the contrary. It is understood that any term in thesingular may include its plural counterpart and vice versa.

As used herein, the term “metathesis catalyst” includes any catalyst orcatalyst system that catalyzes a metathesis reaction.

As used herein, the terms “natural oils,” “natural feedstocks,” or“natural oil feedstocks” may refer to oils derived from plants or animalsources. The term “natural oil” includes natural oil derivatives, unlessotherwise indicated. The terms also include modified plant or animalsources (e.g., genetically modified plant or animal sources), unlessindicated otherwise. Examples of natural oils include, but are notlimited to, vegetable oils, algae oils, fish oils, animal fats, talloils, derivatives of these oils, combinations of any of these oils, andthe like. Representative non-limiting examples of vegetable oils includecanola oil, rapeseed oil, coconut oil, corn oil, cottonseed oil, oliveoil, palm oil, peanut oil, safflower oil, sesame oil, soybean oil,sunflower oil, linseed oil, palm kernel oil, tung oil, jatropha oil,mustard oil, pennycress oil, camelina oil, and castor oil.Representative non-limiting examples of animal fats include lard,tallow, poultry fat, yellow grease, and fish oil. Tall oils areby-products of wood pulp manufacture.

As used herein, the term “natural oil derivatives” may refer to thecompounds or mixture of compounds derived from the natural oil using anyone or combination of methods known in the art. Such methods include butare not limited to saponification, fat splitting, transesterification,esterification, hydrogenation (partial or full), isomerization,oxidation, and reduction. Representative non-limiting examples ofnatural oil derivatives include gums, phospholipids, soapstock,acidulated soapstock, distillate or distillate sludge, fatty acids andfatty acid alkyl ester (e.g. non-limiting examples such as 2-ethylhexylester), hydroxy substituted variations thereof of the natural oil. Forexample, the natural oil derivative may be a fatty acid methyl ester(“FAME”) derived from the glyceride of the natural oil. In someembodiments, a feedstock includes canola or soybean oil, as anon-limiting example, refined, bleached, and deodorized soybean oil(i.e., RBD soybean oil). Soybean oil typically comprises about 95%weight or greater (e.g., 99% weight or greater) triglycerides of fattyacids. Major fatty acids in the polyol esters of soybean oil includesaturated fatty acids, as a non-limiting example, palmitic acid(hexadecanoic acid) and stearic acid (octadecanoic acid), andunsaturated fatty acids, as a non-limiting example, oleic acid(9-octadecenoic acid), linoleic acid (9,12-octadecadienoic acid), andlinolenic acid (9,12,15-octadecatrienoic acid).

As used herein, the term “low-molecular-weight olefin” may refer to anyone or combination of unsaturated straight, branched, or cyclichydrocarbons in the C₂ to C₁₄ range. Low-molecular-weight olefinsinclude “alpha-olefins” or “terminal olefins,” wherein the unsaturatedcarbon-carbon bond is present at one end of the compound.Low-molecular-weight olefins may also include dienes or trienes.Low-molecular-weight olefins may also include internal olefins or“low-molecular-weight internal olefins.” In certain embodiments, thelow-molecular-weight internal olefin is in the C₄ to C₁₄ range. Examplesof low-molecular-weight olefins in the C₂ to C₆ range include, but arenot limited to: ethylene, propylene, 1-butene, 2-butene, isobutene,1-pentene, 2-pentene, 3-pentene, 2-methyl-1-butene, 2-methyl-2-butene,3-methyl-1-butene, cyclopentene, 1,4-pentadiene, 1-hexene, 2-hexene,3-hexene, 4-hexene, 2-methyl-1-pentene, 3-methyl-1-pentene,4-methyl-1-pentene, 2-methyl-2-pentene, 3-methyl-2-pentene,4-methyl-2-pentene, 2-methyl-3-pentene, and cyclohexene. Non-limitingexamples of low-molecular-weight olefins in the C₇ to C₉ range include1,4-heptadiene, 1-heptene, 3,6-nonadiene, 3-nonene, 1,4,7-octatriene.Other possible low-molecular-weight olefins include styrene and vinylcyclohexane. In certain embodiments, it is preferable to use a mixtureof olefins, the mixture comprising linear and branchedlow-molecular-weight olefins in the C₄-C₁₀ range. In one embodiment, itmay be preferable to use a mixture of linear and branched C₄ olefins(i.e., combinations of: 1-butene, 2-butene, and/or isobutene). In otherembodiments, a higher range of C₁₁-C₁₄ may be used.

As used herein, the term “mid-weight olefin” may refer to any one orcombination of unsaturated straight, branched, or cyclic hydrocarbons inthe C₁₅ to C₂₄ range. Mid-weight olefins include “alpha-olefins” or“terminal olefins,” wherein the unsaturated carbon-carbon bond ispresent at one end of the compound. Mid-weight olefins may also includedienes or trienes. Mid-weight olefins may also include internal olefinsor “mid-weight internal olefins.” In certain embodiments, it ispreferable to use a mixture of olefins.

As used herein, the terms “metathesize” and “metathesizing” may refer tothe reacting of a feedstock in the presence of a metathesis catalyst toform a “metathesized product” comprising a new olefinic compound.Metathesizing may refer to cross-metathesis (a.k.a. co-metathesis),self-metathesis, ring-opening metathesis, ring-opening metathesispolymerizations (“ROMP”), ring-closing metathesis (“RCM”), and acyclicdiene metathesis (“ADMET”). As a non-limiting example, metathesizing mayrefer to reacting two triglycerides present in a natural feedstock(self-metathesis) in the presence of a metathesis catalyst, wherein eachtriglyceride has an unsaturated carbon-carbon double bond, therebyforming a new mixture of olefins and esters which may include atriglyceride dimer. Such triglyceride dimers may have more than oneolefinic bond, thus higher oligomers also may form. Additionally,metathesizing may refer to reacting an olefin, such as ethylene, and atriglyceride in a natural feedstock having at least one unsaturatedcarbon-carbon double bond, thereby forming new olefinic molecules aswell as new ester molecules (cross-metathesis).

As used herein, the terms “ester” and “esters” may refer to compoundshaving the general formula: R—COO—R′, wherein R and R′ denote anyorganic compound (such as alkyl, aryl, or silyl groups), including thosebearing heteroatom containing substituent groups. In certainembodiments, R and R′ denote alkyl or aryl groups. In certainembodiments, the term “ester” or “esters” may refer to a group ofcompounds with the general formula described above, wherein thecompounds have different carbon lengths.

As used herein, the term “dibasic ester” may refer to compounds havingthe general formula R′OOC—Y—COO—R″, wherein Y, R′, and R″ denote anyorganic compound (such as alkyl, aryl, or silyl groups), including thosebearing heteroatom containing substituent groups. In certainembodiments, Y is a saturated or unsaturated hydrocarbon, and R′ and R″are alkyl or aryl groups.

As used herein, the term “dibasic acid” may refer to compounds havingthe general formula R′—OOC—Y—COO—R″, wherein R′ and R″ are hydrogen, andY denotes any organic compound (such as an alkyl, aryl, or silyl group),including those bearing heteroatom substituent groups. In certainembodiments, Y is a saturated or unsaturated hydrocarbon.

As used herein, the terms “olefin” and “olefins” may refer tohydrocarbon compounds having at least one unsaturated carbon-carbondouble bond. In certain embodiments, the term “olefin” or “olefins” mayrefer to a group of unsaturated carbon-carbon double bond compounds withdifferent carbon lengths.

It is noted that an olefin may also comprise an ester, and an ester mayalso comprise an olefin, if the R or R′ group in the general formulaR—COO—R′ contains an unsaturated carbon-carbon double bond. For example,a “terminal olefin ester” may refer to an ester compound where R has anolefin positioned at the end of the chain. An “internal olefin ester”may refer to an ester compound where R has an olefin positioned at aninternal location on the chain. Additionally, the term “terminal olefin”may refer to an ester or an acid thereof where R′ denotes hydrogen orany organic compound (such as an alkyl, aryl, or silyl group) and R hasan olefin positioned at the end of the chain, and the term “internalolefin” may refer to an ester or an acid thereof where R′ denoteshydrogen or any organic compound (such as an alkyl, aryl, or silylgroup) and R has an olefin positioned at an internal location on thechain.

As used herein, the terms “paraffin” and “paraffins” may refer tohydrocarbon compounds having only single carbon-carbon bonds, having thegeneral formula C_(n)H_(2n+2), where, in certain embodiments, n isgreater than about 20.

As used herein, the terms “isomerization,” “isomerizes,” or“isomerizing” may refer to the reaction and conversion of straight-chainhydrocarbon compounds, such as normal paraffins, into branchedhydrocarbon compounds, such as iso-paraffins. In other embodiments, theisomerization of an olefin or an unsaturated ester indicates the shiftof the carbon-carbon double bond to another location in the molecule(e.g., conversion from 9-decenoic acid to 8-decenoic acid), or itindicates a change in the geometry of the compound at the carbon-carbondouble bond (e.g., cis to trans). As a non-limiting example, n-pentanemay be isomerized into a mixture of n-pentane, 2-methylbutane, and2,2-dimethylpropane. Isomerization of normal paraffins may be used toimprove the overall properties of a fuel composition. Additionally,isomerization may refer to the conversion of branched paraffins intofurther, more branched paraffins.

As used herein, the term “yield” may refer to the total weight of fuelproduced from the metathesis and hydrogenation reactions. It may alsorefer to the total weight of the fuel following a separation step and/orisomerization reaction. It may be defined in terms of a yield %, whereinthe total weight of the fuel produced is divided by the total weight ofthe natural oil feedstock and, in some embodiments, low-molecular-weightolefin and/or mid-weight olefin, combined.

As used herein, the terms “fuels” and “fuel compositions” refer tomaterials meeting required specifications or to blend components thatare useful in formulating fuel compositions but, by themselves, do notmeet all of the required specifications for a fuel.

As used herein, the term “jet fuel” or “aviation fuel” may refer tokerosene or naphtha-type fuel cuts, or military-grade jet fuelcompositions. “Kerosene-type” jet fuel (including Jet A and Jet A-1) hasa carbon number distribution between about 8 and about 16. Jet A and JetA-1 typically have a flash point of at least approximately 38° C., anauto ignition temperature of approximately 210° C., a freeze point lessthan or equal to approximately −40° C. for Jet A and −47° C. for JetA-1, a density of approximately 0.8 g/cc at 15° C., and an energydensity of approximately 42.8-43.2 MJ/kg. “Naphtha-type” or “wide-cut”jet fuel (including Jet B) has a carbon number distribution betweenabout 5 and about 15. Jet B typically comprises a flash point belowapproximately 0° C., an auto ignition temperature of approximately 250°C., a freeze point of approximately −51° C., a density of approximately0.78 g/cc, and an energy density of approximately 42.8-43.5 MJ/kg.“Military grade” jet fuel refers to the Jet Propulsion or “JP” numberingsystem (JP-1, JP-2, JP-3, JP-4, JP-5, JP-6, JP-7, JP-8, etc.). Militarygrade jet fuels may comprise alternative or additional additives to havehigher flash points than Jet A, Jet A-1, or Jet B in order to cope withheat and stress endured during supersonic flight.

As used herein, the term “diesel fuel” may refer to a hydrocarboncomposition having the following property characteristics, including acarbon number distribution between about 8 and about 25. Diesel fuelsalso typically have a specific gravity of approximately 0.82-1.08 at15.6° C. (60° F.), based on water having a specific gravity of 1 at 60°F. Diesel fuels typically comprise a distillation range betweenapproximately 180-340° C. (356-644° F.). Additionally, diesel fuels havea minimum cetane index number of approximately 40.

As used herein, the term “carbon number distribution” may refer to therange of compounds present in a composition, wherein each compound isdefined by the number of carbon atoms present. As a non-limitingexample, a naphtha-type jet fuel typically comprises a distribution ofhydrocarbon compounds wherein a majority of those compounds have between5 and 15 carbon atoms each. A kerosene-type jet fuel typically comprisesa distribution of hydrocarbon compounds wherein a majority of thosecompounds have between 8 and 16 carbon atoms each. A diesel fueltypically comprises a distribution of hydrocarbon compounds wherein amajority of those compounds have between 8 and 25 carbon atoms each.

As used herein, the term “energy density” may refer to the amount ofenergy stored in a given system per unit mass (MJ/kg) or per unit volume(MJ/L), where MJ refer to million Joules. As a non-limiting example, theenergy density of kerosene- or naphtha-type jet fuel is typicallygreater than about 40 MJ/kg.

In certain embodiments, isomerized acids and/or esters may be formed byproviding an unsaturated fatty acid or fatty acid ester and isomerizingthe unsaturated fatty acid or unsaturated fatty acid ester in thepresence of an isomerization catalyst. In certain embodiments, theunsaturated fatty acid or fatty acid ester comprises a C4-22, C4-C18, orC10-C18 chain (i.e., a C4-C22, C4-C18, or C10-C18 unsaturated fatty acidor unsaturated fatty acid ester). In some embodiments, the unsaturatedfatty acid or fatty acid ester is a C4-C18 unsaturated fatty acid orfatty acid ester. In certain embodiments, the C4-C18 unsaturated fattyacid or fatty acid ester is selected from the group consisting of:pentenoic acid esters, hexenoic acid esters, heptenoic acid esters,octenoic acid esters, nonenoic acid esters, decenoic acid esters,undecenoic acid esters, dodecenoic acid esters, tridecenoic acid esters,tetradecenoic acid esters, pentadecenoic acid esters, hexadecenoic acidesters, heptadecenoic acid esters, octadecenoic acid esters, acidsthereof, and mixtures thereof. In one embodiment, the unsaturated fattyacid or fatty acid ester is 9-dodecenoic acid (9-DDA) or 9-dodecenoicacid methyl ester (9-DDAME).

In certain embodiments, the unsaturated fatty acid or unsaturated fattyacid ester is a terminal olefin having the following structure:

(where X is a C₃-C₁₈ saturated or unsaturated alkyl chain, and R is analkyl group or hydrogen). In certain embodiments, the terminal olefin isselected from the group consisting of: 4-pentenoic acid ester,5-hexenoic acid ester, 6-heptenoic acid ester, 7-octenoic acid ester,8-nonenoic acid ester, 9-decenoic acid ester, 10-undecenoic acid ester,11-dodecenoic acid ester, 12-tridecenoic acid ester, 13-tetradecenoicacid ester, 14-pentadecenoic acid ester, 15-hexadecenoic acid ester,16-heptadecenoic acid ester, 17-octadecenoic acid ester, acids thereof,and mixtures thereof. In one particular embodiment, the terminal olefinis 9-decenoic acid methyl ester (9-DAME) or 9-decenoic acid (9-DA).

In certain embodiments, the unsaturated fatty acid or unsaturated fattyacid ester is derived from transesterifying a natural oil feedstock. Insome embodiments, the transesterification step is prior to or in lieu ofany metathesis reaction of the feedstock. In other embodiments, theunsaturated fatty acid or unsaturated fatty acid ester is derived fromtransesterifying a natural oil feedstock following a metathesis reactionof the natural oil feedstock, which is described in greater detailbelow.

In certain embodiments, the natural oil is sent to a transesterificationunit. Within the transesterification unit, the natural oil is reactedwith at least one alcohol in the presence of a transesterificationcatalyst. In certain embodiments, the alcohol comprises methanol and/orethanol. In another embodiment, the alcohol comprises glycerol (and thetransesterification reaction is a glycerolysis reaction). In oneembodiment, the transesterification reaction is conducted atapproximately 60-70° C. and approximately 1 atm. In certain embodiments,the transesterification catalyst is a homogeneous sodium methoxidecatalyst. Varying amounts of catalyst may be used in the reaction, and,in certain embodiments, the transesterification catalyst is present inthe amount of approximately 0.5-1.0 weight % of the natural oil.

Through the isomerization reaction of the unsaturated fatty acid orunsaturated fatty acid ester, the olefinic double bond can migrate toseveral positions on the carbon chain. For example, isomerization of9-DAME can produce a mixture of products such as x-DAME, wherein x is3-9. Isomerization of 9-DDAME can lead to x-DDAME, wherein x is 3-11.

Isomerization of these fatty acids and/or fatty acid esters may improvevarious performance properties. For example, the isomeric mixtures mayperform better as surfactants because lower CMC (critical micelleconcentration) values are attainable. Further, the isomerized productcomposition may have an observed broadening of the freezing and meltingpoints, which may allow for transportation of the isomerized fattyacid/ester product composition at higher concentrations of the monomerfatty acids and/or monomer fatty acid esters without incurring shippingproblems. In some embodiments, isomerization may reduce the meltingpoint of the starting olefinic composition by at least 5° C., 10° C.,15° C., or 20° C. In other embodiments, isomerization may increase thesolubility of the composition at ambient temperature (i.e., 20-25° C.)by at least 5%, 10%, 15%, 20%, or 25%. In other words, the isomerizatedcomposition may have a solubility that is at least 5%, 10%, 15%, 20%, or25% higher than the solubility of the starting olefinic composition. Insome embodiments, isomerization may increase the solubility atapproximately 0° C. by at least 5%, 10%, or 15%.

In certain embodiments, the isomerization of the acid and/or ester maybe conducted at an elevated temperature (i.e., greater than 25° C.). Incertain embodiments, the temperature of the heat treatment for theisomerization reaction is greater than 100° C., greater than 150° C., orgreater than 200° C. In other embodiments, the temperature is between100° C.-300° C., between 150-250° C., or about 200° C. In someembodiments, the heat treatment step is conducted in the presence of anisomerization catalyst. In one particular embodiment, the isomerizationcatalyst is (PCy₃)₂(Cl)(H)Ru(CO), where “Cy” represents a cyclohexylgroup. In another embodiment, the isomerization catalyst is a sulfonatedtetrafluoroethylene polymer. In one nonlimiting example, the sulfonatedtetrafluoroethylene polymer is a Nafion® resin having the chemicalstructure C₇HF₁₃O₅S.C₂F₄. In another nonlimiting example, the sulfonatedtetrafluoroethylene polymer is Nafion® SAC-13 (CAS 31175-20-9) (i.e.,ethanesulfonic acid,2-[1-[difluoro[(1,2,2-trifluoroethenyl)oxy]methyl]-1,2,2,2-tetrafluoroethoxy]-1,1,2,2-tetrafluoro-,polymer). In certain embodiments, the isomerization catalyst is selectedfrom the group consisting of: a Nafion® resin (available from DuPont,Wilmington, Del., USA), super acids, Amberlyst, perchloric acid,sulfuric acid, phosphoric acid, montmorillonite, zeolites, triflic acid,and combinations thereof.

In certain embodiments, the unsaturated fatty acid or unsaturated fattyacid ester comprises a terminal olefin derived from a natural oilfeedstock (described in greater detail below). In other embodiments, theunsaturated fatty acid or unsaturated fatty acid ester comprises aterminal olefin purchased or produced from an external source separatethan those derived from the natural oil feedstock.

In certain embodiments, prior to the isomerization step, the terminalolefin is metathesized with an internal olefin in the presence of ametathesis catalyst, forming dibasic acids and/or dibasic esters andolefin byproducts. In certain embodiments, the terminal olefin-internalolefin cross-metathesis reaction is conducted at a weight ratio between1:99 (terminal to internal) and 99:1 (terminal to internal). In otherembodiments, the weight ratio of the terminal and internal olefin isbetween 1:5 and 5:1. In yet other embodiments, the weight ratio betweenthe terminal and internal olefin is between 1:2 and 2:1. In oneparticular embodiment, the weight ratio between the terminal andinternal olefin is approximately 1:1.

In certain embodiments, the terminal olefin is selected from the groupconsisting of: 4-pentenoic acid ester, 5-hexenoic acid ester,6-heptenoic acid ester, 7-octenoic acid ester, 8-nonenoic acid ester,9-decenoic acid ester, 10-undecenoic acid ester, 11-dodecenoic acidester, 12-tridecenoic acid ester, 13-tetradecenoic acid ester,14-pentadecenoic acid ester, 15-hexadecenoic acid ester,16-heptadecenoic acid ester, 17-octadecenoic acid ester, acids thereof,and mixtures thereof. In one particular embodiment, the terminal olefinis 9-decenoic acid ester.

In certain embodiments, the internal olefin is selected from the groupconsisting of: pentenoic acid esters, hexenoic acid esters, heptenoicacid esters, octenoic acid esters, nonenoic acid esters, decenoic acidesters, undecenoic acid esters, dodecenoic acid esters, tridecenoic acidesters, tetradecenoic acid esters, pentadecenoic acid esters,hexadecenoic acid esters, heptadecenoic acid esters, octadecenoic acidesters, acids thereof, and mixtures thereof. In one particularembodiment, the internal olefin is 9-undecenoic acid ester. In anotherparticular embodiment, the internal olefin is 9-dodecenoic acid ester.

In some embodiments, the internal olefin is formed by reacting a portionof the terminal olefin ester with a low-molecular-weight internal olefinor mid-weight internal olefin in the presence of a metathesis catalyst.In certain embodiments, the low-molecular-weight internal olefin isselected from the group consisting of: 2-butene, 2-pentene, 2-hexene,3-hexene, 2-heptene, 3-heptene, 2-octene, 3-octene, 4-octene, 2-nonene,3-nonene, 4-nonene, and mixtures thereof. In one particular embodiment,the low-molecular-weight internal olefin is 2-butene. In anotherparticular embodiment, the low-molecular-weight internal olefin is3-hexene.

This process of cross-metathesizing a terminal olefin with an internalolefin may have certain advantages over a self-metathesis reaction tocreate a diacid ester or diacid. For example, the cross-metathesisreaction with an internal olefin helps limit the amount of ethylenebyproduct formed that can potentially poison various metathesiscatalysts. In some instances, this cross-metathesis mechanism allows formild reaction conditions, lower catalyst usage, higher conversion rates,and reduced olefin isomerization byproduct reactions in comparison toself-metathesis mechanisms.

In certain embodiments, at least 70 wt %, 80 wt %, or 90 wt % dibasicester and/or dibasic acid is formed from the cross-metathesis reactionof a terminal olefin and an internal olefin in the presence of less than150 ppm, 100 ppm, 50 ppm, 25 ppm, or ppm catalyst. A comparableself-metathesis reaction with terminal olefins (such as 9-decenoic acidester) under similar reaction conditions may require more catalyst(e.g., more than 150 ppm, or more than 500 ppm) to achieve similaryields of dibasic esters and/or dibasic acids (potentially due to theformation of the ethylene byproduct).

In certain embodiments, the dibasic ester and/or dibasic acid yield isimproved by separating the olefin byproduct formed in thecross-metathesis reaction from the metathesis product while the reactionbetween the terminal olefin and internal olefin is ongoing. In otherembodiments, the dibasic ester and/or dibasic acid yield is improved bysparging the metathesis products in the metathesis reactor with achemically inert gas (e.g., nitrogen, argon, or helium) to ventilatedissolved gases/byproducts (e.g., olefin byproducts) in the metathesisproduct.

In certain embodiments, the cross-metathesis reaction of the terminalolefin and internal olefin produces a dibasic ester comprising thefollowing structure:

wherein R and R′ are independently alkyl, aryl, or silyl groups, and Yis an olefin comprising between 6 and 36 carbon atoms. In oneembodiment, the cross-metathesis reaction forms a dibasic ester, where Rand R′ are methyl and Y is 8-hexadecene (i.e., the dibasic ester formedfrom the cross-metathesis reaction of a terminal olefin and an internalolefin is dimethyl 9-octadecenedioate).

In some embodiments, the dibasic ester may undergo a hydrolysis reactionwith water to form a dibasic acid having the following structure:

wherein Y is an olefin comprising between 6 and 36 carbon atoms. In oneembodiment, Y is 8-hexadecene (i.e., the dibasic acid is 9-octadecenedioic acid). Following hydrolysis, in some embodiments, the productstream may be sent to a flash column or decanter to remove methanol andwater from the diacid.

In other embodiments, the dibasic acid and/or dibasic ester isisomerized to form an isomerized dibasic acid and/or isomerized dibasicester. The isomerization of the dibasic acid and/or dibasic ester may beconducted at an elevated temperature (i.e., greater than 25° C.). Incertain embodiments, the temperature of the heat treatment for theisomerization reaction is greater than 100° C., greater than 150° C., orgreater than 200° C. In other embodiments, the temperature is between100° C.-300° C., between 150-250° C., or about 200° C. In someembodiments, the heat treatment step is conducted in the presence of anisomerization catalyst. Examples of the various types of isomerizationcatalysts are discussed above.

In certain embodiments, the isomerized dibasic acid and/or isomerizeddibasic ester comprises compounds selected from the group consisting of:isomerized dimethyl 9-octadecenedioate or isomerized 9-octadecene dioicacid.

In certain embodiments, the isomerized dibasic acid and/or isomerizeddibasic ester is self-metathesized or cross-metathesized with alow-molecular-weight olefin or mid-weight olefin. Typical metathesisreaction conditions and catalysts are discussed in greater detail below.In one embodiment, the isomerized dibasic acid and/or isomerized dibasicester is self-metathesized in the presence of approximately 10 ppm, 20ppm, 40 ppm, 50 ppm, 80 ppm, 100 ppm, 120 ppm, or greater than 150 ppmmetathesis catalyst.

In certain embodiments, the dibasic acid, dibasic ester, isomerizeddibasic acid, and/or isomerized dibasic ester is hydrogenated. Typicalhydrogenation reaction conditions and catalysts are discussed in greaterdetail below. In one particular example, the hydrogenation reaction isconducted in the presence of a nickel based catalyst at approximately150° C. and 150 psig.

In certain embodiments, the dibasic acids, dibasic esters, isomerizeddibasic acids, and/or isomerized dibasic esters may be used in a varietyof different commercial applications, including, but not limited to:lubricants, waxes, films, paints, paint strippers, coatings,plasticizers, resins, binders, solvents, polyols, soil stabilization,chemical grouting, oilfield drilling fluids, crop protection products,surfactants, intermediates, and adhesives.

As mentioned above, the terminal olefin and internal olefin may bederived from a natural oil feedstock, in addition to other valuablecompositions. A number of valuable compositions may be targeted throughthe self-metathesis reaction of a natural oil feedstock, or thecross-metathesis reaction of the natural oil feedstock with alow-molecular-weight olefin or mid-weight olefin, in the presence of ametathesis catalyst. Such valuable compositions may include fuelcompositions, detergents, surfactants, and other specialty chemicals.Non-limiting examples of fuel compositions include jet, kerosene, anddiesel fuel. Additionally, transesterified products (i.e., the productsformed from transesterifying an ester in the presence of an alcohol) mayalso be targeted, non-limiting examples of which include: fatty acidmethyl esters; biodiesel; 9-decenoic acid (“9DA”) esters, 9-undecenoicacid (“9UDA”) esters, and/or 9-dodecenoic acid (“9DDA”) esters; 9DA,9UDA, and/or 9DDA; alkali metal salts and alkaline earth metal salts of9DA, 9UDA, and/or 9DDA; dimers of the transesterified products; andmixtures thereof.

In certain embodiments, prior to a metathesis reaction, a natural oilfeedstock may be treated to render the natural oil more suitable for thesubsequent metathesis reaction. In certain embodiments, the natural oilpreferably is a vegetable oil or vegetable oil derivative, such assoybean oil.

In one embodiment, the treatment of the natural oil involves the removalof catalyst poisons, such as peroxides, which may potentially diminishthe activity of the metathesis catalyst. Non-limiting examples ofnatural oil feedstock treatment methods to diminish catalyst poisonsinclude those described in PCT/US2008/09604, PCT/US2008/09635, and U.S.patent application Ser. Nos. 12/672,651 and 12/672,652, hereinincorporated by reference in their entireties. In certain embodiments,the natural oil feedstock is thermally treated by heating the feedstockto a temperature greater than 100° C. in the absence of oxygen and heldat the temperature for a time sufficient to diminish catalyst poisons inthe feedstock. In other embodiments, the temperature is betweenapproximately 100° C. and 300° C., between approximately 120° C. and250° C., between approximately 150° C. and 210° C., or approximatelybetween 190 and 200° C. In one embodiment, the absence of oxygen isachieved by sparging the natural oil feedstock with nitrogen, whereinthe nitrogen gas is pumped into the feedstock treatment vessel at apressure of approximately 10 atm (150 psig).

In certain embodiments, the natural oil feedstock is chemically treatedunder conditions sufficient to diminish the catalyst poisons in thefeedstock through a chemical reaction of the catalyst poisons. Incertain embodiments, the feedstock is treated with a reducing agent or acation-inorganic base composition. Non-limiting examples of reducingagents include bisulfite, borohydride, phosphine, thiosulfate,individually or combinations thereof.

In certain embodiments, the natural oil feedstock is treated with anadsorbent to remove catalyst poisons. In one embodiment, the feedstockis treated with a combination of thermal and adsorbent methods. Inanother embodiment, the feedstock is treated with a combination ofchemical and adsorbent methods. In another embodiment, the treatmentinvolves a partial hydrogenation treatment to modify the natural oilfeedstock's reactivity with the metathesis catalyst. Additionalnon-limiting examples of feedstock treatment are also described belowwhen discussing the various metathesis catalysts.

Additionally, in certain embodiments, the low-molecular-weight olefin ormid-weight olefin may also be treated prior to the metathesis reactionwith the natural oil. Like the natural oil treatment, thelow-molecular-weight olefin or mid-weight olefin may be treated toremove poisons that may impact or diminish catalyst activity.

In certain embodiments, the low-molecular-weight olefin or mid-weightolefin may be self-metathesized to form a metathesizedlow-molecular-weight olefin or metathesized mid-weight olefin in orderto adjust the properties of the olefin and the potential productsfollowing metathesis with the natural oil. In some embodiments, thelow-molecular-weight olefin or mid-weight olefin is self-metathesized inthe presence of a rhenium oxide catalyst (e.g., rhenium oxide supportedon alumina) or tungsten oxide catalyst (e.g., tungsten oxide supportedon silica). This reaction may be conducted in a fixed bed reactor. Inone embodiment, the low-molecular-weight olefin is 1-butene. Thelow-molecular-weight olefin may be self-metathesized over rhenium oxidecatalyst in a fixed bed reactor to produce mainly 3-hexene and ethylene.Ethylene may be separated from the reactor effluent for furtherprocessing, such as being sent to an ethylene purification system orethylene oxide system. Unreacted low-molecular-weight olefin (e.g.,1-butene) may be recycled to the fixed bed reactor and the metathesizedlow-weight-olefin (e.g., 3-hexene) may be sent to the metathesis reactorfor metathesis with the natural oil.

In other embodiments, the low-molecular-weight olefin or mid-weightolefin is isomerized prior to being metathesized with the natural oil.Adjusting the composition and properties of the low-molecular-weightolefin or mid-weight olefin through isomerization may allow fordifferent products or different ratios of products to be formedfollowing metathesis of the low-molecular-weight olefin or mid-weightolefin with a natural oil. In some embodiments, the isomerized orbranched low-molecular-weight olefin is in the C₄ to C₁₀ range. In oneembodiment, hexene is isomerized to form a branched low-molecular-weightolefin. Non-limiting examples of branched low-molecular-weight olefinsinclude isobutene, 3-methyl-1-butene, 2-methyl-3-pentene, and2,2-dimethyl-3-pentene.

By using branched low-molecular-weight olefins or branched mid-weightolefins in the metathesis reaction, the metathesized product willinclude branched olefins, which can be subsequently hydrogenated toiso-paraffins. In certain embodiments, the branched low-molecular-weightolefins or branched mid-weight olefins may help achieve the desiredperformance properties for a fuel composition, such as jet, kerosene, ordiesel fuel. In certain embodiments, C₁₁-C₁₄ olefins may be targetedfollowing metathesis and separation steps through isomerization of thelow-molecular-weight olefin. In other embodiments, the branchedlow-molecular-weight olefins or branched mid-weight olefins may helptarget longer chain esters for use as detergents or cleaningcompositions. In some embodiments, C₁₀-C₁₅ or C₁₁-C₁₄ methyl esters maybe targeted following metathesis, separation, and transesterificationsteps (discussed in detail below). Isomerization reactions arewell-known in the art, as described in U.S. Pat. Nos. 3,150,205;4,210,771; 5,095,169; and 6,214,764, herein incorporated by reference intheir entireties.

As shown in FIG. 1, after this optional treatment of the natural oilfeedstock, low-molecular-weight olefin, and/or mid-weight olefin, thenatural oil 12 is reacted with itself, or combined with alow-molecular-weight olefin 14 or mid-weight olefin 15 in a metathesisreactor 20 in the presence of a metathesis catalyst. Metathesiscatalysts and metathesis reaction conditions are discussed in greaterdetail below. In certain embodiments, in the presence of a metathesiscatalyst, the natural oil 12 undergoes a self-metathesis reaction withitself. In other embodiments, in the presence of the metathesiscatalyst, the natural oil 12 undergoes a cross-metathesis reaction withthe low-molecular-weight olefin 14 or mid-weight olefin 15. In certainembodiments, the natural oil 12 undergoes both self- andcross-metathesis reactions in parallel metathesis reactors. Theself-metathesis and/or cross-metathesis reaction form a metathesizedproduct 22 wherein the metathesized product 22 comprises olefins 32 andesters 34.

In certain embodiments, the low-molecular-weight olefin 14 is in the C₂to C₆ range. As a non-limiting example, in one embodiment, thelow-molecular-weight olefin 14 may comprise at least one of thefollowing: ethylene, propylene, 1-butene, 2-butene, isobutene,1-pentene, 2-pentene, 3-pentene, 2-methyl-1-butene, 2-methyl-2-butene,3-methyl-1-butene, cyclopentene, 1,4-pentadiene, 1-hexene, 2-hexene,3-hexene, 4-hexene, 2-methyl-1-pentene, 3-methyl-1-pentene,4-methyl-1-pentene, 2-methyl-2-pentene, 3-methyl-2-pentene,4-methyl-2-pentene, 2-methyl-3-pentene, and cyclohexene. Non-limitingexamples of low-molecular-weight olefins in the C₇ to C₉ range include1,4-heptadiene, 1-heptene, 3,6-nonadiene, 3-nonene, 1,4,7-octatriene. Inanother embodiment, the low-molecular-weight olefin 14 comprises atleast one of styrene and vinyl cyclohexane. In another embodiment, thelow-molecular-weight olefin 14 may comprise at least one of ethylene,propylene, 1-butene, 2-butene, and isobutene. In another embodiment, thelow-molecular-weight olefin 14 comprises at least one alpha-olefin orterminal olefin in the C₂ to C₁₀ range.

In another embodiment, the low-molecular-weight olefin 14 comprises atleast one branched low-molecular-weight olefin in the C₄ to C₁₀ range.Non-limiting examples of branched low-molecular-weight olefins includeisobutene, 3-methyl-1-butene, 2-methyl-3-pentene, and2,2-dimethyl-3-pentene.

In certain embodiments, the mid-weight olefin 15 comprises unsaturatedstraight, branched, or cyclic hydrocarbons in the C₁₅ to C₂₄ range. Insome embodiments, the mid-weight olefin is an alpha-olefin or terminalolefin.

As noted, it is possible to use a mixture of various linear or branchedlow-molecular-weight olefins and linear or branched mid-weight olefinsin the reaction to achieve the desired metathesis product distribution.In certain embodiments, the mixture comprises linear and/or branchedlow-molecular-weight olefins. In other embodiments, the mixturecomprises linear and/or branched mid-weight olefins. In one embodiment,a mixture of butenes (1-butene, 2-butenes, and, optionally, isobutene)may be employed as the low-molecular-weight olefin, offering a low cost,commercially available feedstock instead a purified source of oneparticular butene. Such low cost mixed butene feedstocks are typicallydiluted with n-butane and/or isobutane.

In certain embodiments, recycled streams from downstream separationunits may be introduced to the metathesis reactor 20 in addition to thenatural oil 12 and, in some embodiments, the low-molecular-weight olefin14 and/or mid-weight olefin 15. For instance, in some embodiments, aC₂-C₆ recycle olefin stream or a C₃-C₄ bottoms stream from an overheadseparation unit may be returned to the metathesis reactor. In oneembodiment, as shown in FIG. 1, a light weight olefin stream 44 from anolefin separation unit 40 may be returned to the metathesis reactor 20.In another embodiment, the C₃-C₄ bottoms stream and the light weightolefin stream 44 are combined together and returned to the metathesisreactor 20. In another embodiment, a C₁₅₊ bottoms stream 46 from theolefin separation unit 40 is returned to the metathesis reactor 20. Inanother embodiment, all of the aforementioned recycle streams arereturned to the metathesis reactor 20.

In other embodiments, various ester streams downstream of thetransesterification unit (discussed below) may also be recycled orreturned to the metathesis reactor 20. In certain embodiments, aglycerolysis reaction may be conducted on the recycled ester stream toprevent or limit the amount of free glycerol entering the metathesisreactor 20. In some embodiments, the recycled ester stream will undergoa purification step to limit the amount of methanol being recycled tothe metathesis reactor 20. In some embodiments, the recycled esterstream is combined with the low-molecular-weight olefin 14 and/ormid-weight olefin 15 prior to conducting the glycerolysis reaction andentering the metathesis reactor 20. The glycerolysis reaction may alsolimit or prevent free fatty acid methyl esters from entering themetathesis reaction and subsequently exiting the metathesis reactor asfree fatty acid methyl esters that may boil close to various high-valuedolefin products. In such cases, these methyl ester components may beseparated with the olefins during the separation of the olefins andesters. Such methyl ester components may be difficult to separate fromthe olefins by distillation.

The metathesis reaction in the metathesis reactor 20 produces ametathesized product 22. In one embodiment, the metathesized product 22enters a flash vessel operated under temperature and pressure conditionswhich target C₂ or C₂-C₃ compounds to flash off and be removed overhead.The C₂ or C₂-C₃ light ends are comprised of a majority of hydrocarboncompounds having a carbon number of 2 or 3. In certain embodiments, theC₂ or C₂-C₃ light ends are then sent to an overhead separation unit,wherein the C₂ or C₂-C₃ compounds are further separated overhead fromthe heavier compounds that flashed off with the C₂-C₃ compounds. Theseheavier compounds are typically C₃-C₅ compounds carried overhead withthe C₂ or C₂-C₃ compounds. After separation in the overhead separationunit, the overhead C₂ or C₂-C₃ stream may then be used as a fuel source.These hydrocarbons have their own value outside the scope of a fuelcomposition, and may be used or separated at this stage for other valuedcompositions and applications. In certain embodiments, the bottomsstream from the overhead separation unit containing mostly C₃-C₅compounds is returned as a recycle stream to the metathesis reactor. Inthe flash vessel, the metathesized product 22 that does not flashoverhead is sent downstream for separation in a separation unit 30, suchas a distillation column.

Prior to the separation unit 30, in certain embodiments, themetathesized product 22 may be contacted with a reactant or reagent todeactivate or to extract the catalyst. In certain embodiments, themetathesized product 22 is introduced to an adsorbent or complexingagent to facilitate the separation of the metathesized product 22 fromthe metathesis catalyst. In one embodiment, the adsorbent or complexingagent is a clay bed. The clay bed will adsorb the metathesis catalyst,and after a filtration step, the metathesized product 22 can be sent tothe separation unit 30 for further processing. In another embodiment,the adsorbent or complexing agent is a water soluble phosphine reagentsuch as tris hydroxymethyl phosphine (THMP). Catalyst may be separatedwith a water soluble phosphine through known liquid-liquid extractionmechanisms by decanting the aqueous phase from the organic phase.

In some embodiments, the metathesized product 22 may be sent to acatalyst kill drum where the reagent (e.g., THMP aqueous solution) isadded to deactivate the metathesis catalyst. THMP may be added at a rateequivalent to at least 1:1, 5:1, 10:1, 25:1, or 50:1 molar ratiorelative to the catalyst pumped into the catalyst kill drum.

In certain embodiments, the reagent (e.g., THMP) can be left in themetathesized product 22 and carried along, either in whole or in part,into a subsequent chemical reaction or processing step. In otherembodiments, the reagent can be separated and removed from the mixture,either partially or completely, prior to any subsequent reaction orprocessing step. In some embodiments, passivation and extraction can becoupled into one step (e.g., by providing the reagent in the extractingmaterial).

In one embodiment, the catalyst separation occurs by sending theeffluent from the catalyst kill drum to a catalyst decanter drum. Thedecanter drum may function as a horizontal vessel with a vertical baffleand a boot to collect the water phase containing the metathesiscatalyst. In some embodiments, the decanter drum operates at atemperature between approximately 60-90° C. and a pressure between 1-1.5atm, or approximately 53° C. (127° F.) and 1.1 atm (16 psia).

In other embodiments, the catalyst separation comprises washing orextracting the mixture with a polar solvent (e.g., particularly, thoughnot exclusively, for embodiments in which the reagent is at leastpartially soluble in the polar solvent). In some embodiments, the polarsolvent is added in a subsequent step following catalyst deactivation.In other embodiments, the polar solvent (e.g., water) is added to themetathesized product 22 at approximately the same time as thedeactivation reagent (e.g., THMP). Near simultaneous addition of thedeactivation reagent and polar solvent to the metathesized product caneliminate the need for an additional reaction/separation vessel, whichmay simply the process and potentially save capital.

In some embodiments, the polar solvent is at least partiallynon-miscible with the mixture, such that a separation of layers canoccur. In some embodiments, at least a portion of the reagent ispartitioned into the polar solvent layer, which can then be separatedfrom the non-miscible remaining layer and removed. Representative polarsolvents for use in accordance with the present teachings include butare not limited to water, alcohols (e.g., methanol, ethanol, etc.),ethylene glycol, glycerol, DMF, multifunctional polar compoundsincluding but not limited to polyethylene glycols and/or glymes, ionicliquids, and the like, and combinations thereof. In some embodiments,the mixture is extracted with water. In some embodiments, when aphosphite ester that is at least partially hydrolyzable (e.g., in someembodiments, a phosphite ester having a low molecular weight, includingbut not limited to trimethyl phosphite, triethyl phosphite, and acombination thereof) is used as a reagent, washing the mixture withwater may convert the phosphite ester into a corresponding acid. Whileneither desiring to be bound by any particular theory nor intending tolimit in any measure the scope of the appended claims or theirequivalents, it is presently believed that such a hydrolysis may occurmore rapidly with lower molecular weight esters.

In some embodiments, when extraction with a polar solvent is desired,the extracting may comprise high shear mixing (e.g., mixing of a typesufficient to disperse and/or transport at least a portion of a firstphase and/or chemical species into a second phase with which the firstphase and/or a chemical species would normally be at least partlyimmiscible) although such mixing, in some embodiments, may contribute toundesirable emulsion formation. In some embodiments, the extractingcomprises low-intensity mixing (e.g., stirring that is not high shear).The present teachings are in no way restricted to any particular type orduration of mixing. However, for purposes of illustration, in someembodiments, the extracting comprises mixing the polar solvent and themixture together for at least about 1 second, 10 seconds, 30 seconds, 1minute, 2 minutes, 5 minutes, 10 minutes, 15 minutes, 20 minutes, 25minutes, 30 minutes, 35 minutes, 40 minutes, 45 minutes, 50 minutes, 55minutes, or 60 minutes. While neither desiring to be bound by anyparticular theory nor intending to limit in any measure the scope of theappended claims or their equivalents, it is presently believed thatshorter mixing times (e.g., on the order of a second or seconds) areachievable when inline shear mixing is used for mixing.

When extraction with a polar solvent is desired, the present teachingsare in no way restricted to any particular amount of polar solvent addedto the mixture for the extracting. However, for purposes ofillustration, in some embodiments, the amount by weight of polar solvent(e.g., water) added to the mixture for the extracting is more than theweight of the mixture. In some embodiments, the amount by weight ofpolar solvent (e.g., water) added to the mixture for the extracting isless than the weight of the mixture. In some embodiments, the weightratio of the mixture to the water added to the mixture is at least about1:1, 2:1, 3:1, 4:1, 5:1, 6:1, 7:1, 8:1, 9:1, 10:1, 20:1, 40:1, or 100:1.For higher oil to water ratios, extraction and separation using acentrifuge and/or coalescer may be desirable.

In some embodiments, when extraction with a polar solvent is desired,methods for suppressing dehydrogenation in accordance with the presentteachings further comprise allowing a settling period following thepolar solvent wash to promote phase separation. The present teachingsare in no way restricted to any particular duration of settling period.However, for purposes of illustration, in some embodiments, the settlingperiod is at least about 1 minute, 2 minutes, 5 minutes, 10 minutes, 15minutes, 30 minutes, 60 minutes, or 120 minutes.

In addition to or as an alternative to washing the mixture with a polarsolvent to remove the reagent (e.g., THMP)—a method in accordance withthe present teachings can optionally further comprise removing at leasta portion of the reagent by adsorbing it onto an adsorbent, whichoptionally can then be physically separated from the mixture (e.g., viafiltration, centrifugation, crystallization, or the like). In someembodiments, the adsorbent is polar. Representative adsorbents for usein accordance with the present teachings include but are not limited tocarbon, silica, silica-alumina, alumina, clay, magnesium silicates(e.g., Magnesols), the synthetic silica adsorbent sold under thetradename TRISYL by W. R. Grace & Co., diatomaceous earth, polystyrene,macroporous (MP) resins, and the like, and combinations thereof.

Additionally, in certain embodiments, prior to the separation unit 30(and after catalyst separation, in some instances), the metathesisproduct 22 may be sent to a hydrogenation unit, wherein thecarbon-carbon double bonds in the olefins and esters are partially tofully saturated with hydrogen gas. Hydrogenation may be conductedaccording to any known method in the art for hydrogenating doublebond-containing compounds such as the olefins and esters present in themetathesis product 22. In certain embodiments, in the hydrogenationunit, hydrogen gas is reacted with the metathesis product 22 in thepresence of a hydrogenation catalyst to produce a hydrogenated productcomprising partially to fully hydrogenated paraffins/olefins andpartially to fully hydrogenated esters.

In some embodiments, the metathesis product 22 is hydrogenated in thepresence of a hydrogenation catalyst comprising nickel, copper,palladium, platinum, molybdenum, iron, ruthenium, osmium, rhodium, oriridium, individually or in combinations thereof. Useful catalyst may beheterogeneous or homogeneous. In some embodiments, the catalysts aresupported nickel or sponge nickel type catalysts.

In some embodiments, the hydrogenation catalyst comprises nickel thathas been chemically reduced with hydrogen to an active state (i.e.,reduced nickel) provided on a support. The support may comprise poroussilica (e.g., kieselguhr, infusorial, diatomaceous, or siliceous earth)or alumina. The catalysts are characterized by a high nickel surfacearea per gram of nickel.

Commercial examples of supported nickel hydrogenation catalysts includethose available under the trade designations “NYSOFACT”, “NYSOSEL”, and“NI 5248 D” (from BASF Catalysts LLC, Iselin, N.J.). Additionalsupported nickel hydrogenation catalysts include those commerciallyavailable under the trade designations “PRICAT 9910”, “PRICAT 9920”,“PRICAT 9908”, “PRICAT 9936” (from Johnson Matthey Catalysts, Ward Hill,Mass.).

The supported nickel catalysts may be of the type described in U.S. Pat.No. 3,351,566, U.S. Pat. No. 6,846,772, EP 0168091, and EP 0167201,incorporated by reference herein in their entireties. Hydrogenation maybe carried out in a batch or in a continuous process and may be partialhydrogenation or complete hydrogenation. In certain embodiments, thetemperature ranges from about 50° C. to about 350° C., about 100° C. toabout 300° C., about 150° C. to about 250° C., or about 100° C. to about150° C. The desired temperature may vary, for example, with hydrogen gaspressure. Typically, a higher gas pressure will require a lowertemperature. Hydrogen gas is pumped into the reaction vessel to achievea desired pressure of H₂ gas. In certain embodiments, the H₂ gaspressure ranges from about 15 psig (1 atm) to about 3000 psig (204.1atm), about 15 psig (1 atm) to about 90 psig (6.1 atm), or about 100psig (6.8 atm) to about 500 psig (34 atm). As the gas pressureincreases, more specialized high-pressure processing equipment may berequired. In certain embodiments, the reaction conditions are “mild,”wherein the temperature is approximately between approximately 50° C.and approximately 100° C. and the H₂ gas pressure is less thanapproximately 100 psig. In other embodiments, the temperature is betweenabout 100° C. and about 150° C., and the pressure is between about 100psig (6.8 atm) and about 500 psig (34 atm). When the desired degree ofhydrogenation is reached, the reaction mass is cooled to the desiredfiltration temperature.

The amount of hydrogenation catalyst is typically selected in view of anumber of factors including, for example, the type of hydrogenationcatalyst used, the amount of hydrogenation catalyst used, the degree ofunsaturation in the material to be hydrogenated, the desired rate ofhydrogenation, the desired degree of hydrogenation (e.g., as measure byiodine value (IV)), the purity of the reagent, and the H₂ gas pressure.In some embodiments, the hydrogenation catalyst is used in an amount ofabout 10 weight % or less, for example, about 5 weight % or less orabout 1 weight % or less.

When the desired degree of hydrogenation is reached, the reaction massis cooled to the desired filtration temperature. During hydrogenation,the carbon-carbon double bonds are partially to fully saturated by thehydrogen gas. In one embodiment, the olefins in the metathesis product22 are reacted with hydrogen to form a fuel composition comprising onlyor mostly paraffins. Additionally, the esters from the metathesisproduct are fully or nearly fully saturated in the hydrogenation unit.In another embodiment, the resulting hydrogenated product includes onlypartially saturated paraffins/olefins and partially saturated esters.

In the separation unit 30, in certain embodiments, the metathesizedproduct 22 (from a hydrogenation unit, metathesis reactor 20, orcatalyst separation unit) is separated into at least two productstreams. In one embodiment, the metathesized product 22 is sent to theseparation unit 30, or distillation column, to separate the olefins 32from the esters 34. In another embodiment, a byproduct stream comprisingC₇'s and cyclohexadienes (e.g., 1,4-cyclohexadiene) may be removed in aside-stream from the separation unit 30. In certain embodiments, theseparated olefins 32 may comprise hydrocarbons with carbon numbers up to24. In certain embodiments, the esters 34 may comprise metathesizedglycerides. In other words, the lighter end olefins 32 are preferablyseparated or distilled overhead for processing into olefin compositions,while the esters 34, comprised mostly of compounds having carboxylicacid/ester functionality, are drawn into a bottoms stream. Based on thequality of the separation, it is possible for some ester compounds to becarried into the overhead olefin stream 32, and it is also possible forsome heavier olefin hydrocarbons to be carried into the ester stream 34.Additionally, the separated cyclohexadienes (e.g., 1,4-cyclohexadiene)may be further processed in a dehydrogenation step to form benzene.Examples of catalytic dehydrogenation catalysts include platinumsupported on alumina. Examples of oxidative dehydrogenation catalystsinclude mixed metal oxides consisting of molybdenum, vanadium, niobium,tellurium, magnesium, and/or aluminum. Other dehydrogenation catalystsexamples include cerium/zirconium, alkaline earth/nickel,calcium-nickel-phosphate, chromium, iron-chromium oxide,bismuth/molybdenum, tin/antimony, silver, copper.

In one embodiment, the olefins 32 may be collected and sold for anynumber of known uses. In other embodiments, the olefins 32 are furtherprocessed in an olefin separation unit 40 and/or hydrogenation unit 50(where the olefinic bonds are saturated with hydrogen gas 48, asdescribed below). In other embodiments, esters 34 comprising heavier endglycerides and free fatty acids are separated or distilled as a bottomsproduct for further processing into various products. In certainembodiments, further processing may target the production of thefollowing non-limiting examples: fatty acid methyl esters; biodiesel;9DA esters, 9UDA esters, and/or 9DDA esters; 9DA, 9UDA, and/or 9DDA;alkali metal salts and alkaline earth metal salts of 9DA, 9UDA, and/or9DDA; diacids, and/or diesters of the transesterified products; andmixtures thereof. In certain embodiments, further processing may targetthe production of C₁₅-C₁₈ fatty acids and/or esters. In otherembodiments, further processing may target the production of diacidsand/or diesters. In yet other embodiments, further processing may targetthe production of compounds having molecular weights greater than themolecular weights of stearic acid and/or linolenic acid.

As shown in FIG. 1, regarding the overhead olefins 32 from theseparation unit 30, the olefins 32 may be further separated or distilledin the olefin separation unit 40 to separate the various compositions.The olefin separation unit 40 may comprise a number of distillationtowers. In some embodiments, the various composition streams areseparated using at least four distillation towers. In other embodiments,three towers or less are used to separate the olefin compositions.

In one embodiment, light end olefins 44 consisting of mainly C₂-C₉compounds may be distilled into an overhead stream from the olefinseparation unit 40. In certain embodiments, the light end olefins 44 arecomprised of a majority of C₃-C₈ hydrocarbon compounds. In otherembodiments, heavier olefins having higher carbon numbers may beseparated overhead into the light end olefin stream 44 to assist intargeting a specific fuel composition. The light end olefins 44 may berecycled to the metathesis reactor 20, purged from the system forfurther processing and sold, or a combination of the two. In oneembodiment, the light end olefins 44 may be partially purged from thesystem and partially recycled to the metathesis reactor 20. With regardsto the other streams in the olefin separation unit 40, a heavier C₁₆₊,C₁₈₊, C₂₀₊, C₂₂₊, or C₂₄₊ compound stream may be separated out as anolefin bottoms stream 46. This olefin bottoms stream 46 may be purged orrecycled to the metathesis reactor 20 for further processing, or acombination of the two. In another embodiment, a center-cut olefinstream 42 may be separated out of the olefin distillation unit forfurther processing. The center-cut olefins 42 may be designed to targeta selected carbon number range for a specific fuel composition. As anon-limiting example, a C₅-C₁₅ distribution may be targeted for furtherprocessing into a naphtha-type jet fuel. Alternatively, a C₈-C₁₆distribution may be targeted for further processing into a kerosene-typejet fuel. In another embodiment, a C₈-C₂₅ distribution may be targetedfor further processing into a diesel fuel.

In some embodiments, processing steps may be conducted to maximize alphaolefin purity. In other embodiments, processing steps may be conductedto maximize C₁₀ olefin purity. For example, C₁₀₊ olefins from theseparation unit 30 or a particular olefin stream may be reacted withethylene in the presence of a metathesis catalyst in a secondarymetathesis reactor to improve the C₁₀ olefin purity. In one embodiment,the metathesis catalyst is a rhenium oxide catalyst (e.g., rhenium oxidesupported on alumina). In another embodiment, the metathesis is atungsten oxide catalyst (e.g., tungsten oxide supported on silica). Thismetathesis reaction may be conducted in a fixed bed reactor. In someembodiments, the ethylene reagent can be recycled back to the secondarymetathesis reactor. Lighter olefins (C₄-C₉) from the secondarymetathesis reactor may be mixed with the main metathesis reactor olefinsfrom the separation unit 30 for further processing.

In certain embodiments, the olefins 32 may be oligomerized to formpoly-alpha-olefins (PAOs) or poly-internal-olefins (PIOs), mineral oilsubstitutes, and/or biodiesel fuel. The oligomerization reaction maytake place after the distillation unit 30 or after the overhead olefinseparation unit 40. In certain embodiments, byproducts from theoligomerization reactions may be recycled back to the metathesis reactor20 for further processing.

In other embodiments, the olefins 32, light end olefins 44, orcenter-cut olefins 42 may be self-metathesized in the presence of ametathesis catalyst in a secondary metathesis reactor in order toproduce heavier weight C₁₄₊, C₁₆₊, or C₁₈₊ olefin products. In oneembodiment, the metathesis catalyst is a rhenium oxide catalyst (e.g.,rhenium oxide supported on alumina). In another embodiment, themetathesis is a tungsten oxide catalyst (e.g., tungsten oxide supportedon silica). This metathesis reaction may be conducted in a fixed bedreactor. The heavier weight C₁₄₊, C₁₆₊, or C₁₈₊ olefins may be used assurfactants or oil lubes. In some embodiments, the lighter olefinbyproducts from the self-metathesis reaction may be recycled back to thesecondary metathesis reactor or primary metathesis reactor 20 forfurther processing.

As mentioned, in one embodiment, the olefins 32 from the separation unit30 may be sent directly to the hydrogenation unit 50. In anotherembodiment, the center-cut olefins 42 from the overhead olefinseparation unit 40 may be sent to the hydrogenation unit 50.Hydrogenation may be conducted according to any known method in the artfor hydrogenating double bond-containing compounds such as the olefins32 or center-cut olefins 42. In certain embodiments, in thehydrogenation unit 50, hydrogen gas 48 is reacted with the olefins 32 orcenter-cut olefins 42 in the presence of a hydrogenation catalyst toproduce a hydrogenated product 52.

Typical hydrogenation catalysts and reaction conditions are discussedabove. During hydrogenation, the carbon-carbon double bond containingcompounds in the olefins are partially to fully saturated by thehydrogen gas 48. In one embodiment, the resulting hydrogenated product52 includes hydrocarbons with a distribution centered betweenapproximately C₁₀ and C₁₂ hydrocarbons for naphtha- and kerosene-typejet fuel compositions. In another embodiment, the distribution iscentered between approximately C₁₆ and C₁₈ for a diesel fuelcomposition.

In certain embodiments, after hydrogenation, the hydrogenation catalystmay be removed from the hydrogenated product 52 using known techniquesin the art, for example, by filtration. In some embodiments, thehydrogenation catalyst is removed using a plate and frame filter such asthose commercially available from Sparkler Filters, Inc., Conroe Tex. Insome embodiments, the filtration is performed with the assistance ofpressure or a vacuum. In order to improve filtering performance, afilter aid may be used. A filter aid may be added to the productdirectly or it may be applied to the filter. Representative non-limitingexamples of filtering aids include diatomaceous earth, silica, alumina,and carbon. Typically, the filtering aid is used in an amount of about10 weight % or less, for example, about 5 weight % or less or about 1weight % or less. Other filtering techniques and filtering aids also maybe employed to remove the used hydrogenation catalyst. In otherembodiments the hydrogenation catalyst is removed using centrifugationfollowed by decantation of the product.

In certain embodiments, based upon the quality of the hydrogenatedproduct 52 produced in the hydrogenation unit 50, it may be preferableto isomerize the olefin hydrogenated product 52 to assist in targetingof desired fuel properties such as flash point, freeze point, energydensity, cetane number, or end point distillation temperature, amongother parameters. Isomerization reactions are well-known in the art, asdescribed in U.S. Pat. Nos. 3,150,205; 4,210,771; 5,095,169; and6,214,764, herein incorporated by reference in their entireties. In oneembodiment, the isomerization reaction at this stage may also crack someof the C₁₅₊ compounds remaining, which may further assist in producing afuel composition having compounds within the desired carbon numberrange, such as 5 to 16 for a jet fuel composition.

In certain embodiments, the isomerization may occur concurrently withthe hydrogenation step in the hydrogenation unit 50, thereby targeting adesired fuel product. In other embodiments, the isomerization step mayoccur before the hydrogenation step (i.e., the olefins 32 or center-cutolefins 42 may be isomerized before the hydrogenation unit 50). In yetother embodiments, it is possible that the isomerization step may beavoided or reduced in scope based upon the selection oflow-molecular-weight olefin(s) 14 and/or mid-weight olefin(s) 15 used inthe metathesis reaction.

In certain embodiments, the hydrogenated product 52 comprisesapproximately 15-25 weight % C₇, approximately <5 weight % C₈,approximately 20-40 weight % C₉, approximately 20-40 weight % C₁₀,approximately <5 weight % C₁₁, approximately 15-25 weight % C₁₂,approximately <5 weight % C₁₃, approximately <5 weight % C₁₄,approximately <5 weight % C₁₅, approximately <1 weight % C₁₆,approximately <1 weight % C₁₇, and approximately <1 weight % C₁₈₊. Incertain embodiments, the hydrogenated product 52 comprises a heat ofcombustion of at least approximately 40, 41, 42, 43 or 44 MJ/kg (asmeasured by ASTM D3338). In certain embodiments, the hydrogenatedproduct 52 contains less than approximately 1 mg sulfur per kghydrogenated product (as measured by ASTM D5453). In other embodiments,the hydrogenated product 52 comprises a density of approximately0.70-0.75 (as measured by ASTM D4052). In other embodiments, thehydrogenated product has a final boiling point of approximately 220-240°C. (as measured by ASTM D86).

The hydrogenated product 52 produced from the hydrogenation unit 50 maybe used as a fuel composition, non-limiting examples of which includejet, kerosene, or diesel fuel. In certain embodiments, the hydrogenatedproduct 52 may contain byproducts from the hydrogenation, isomerization,and/or metathesis reactions. As shown in FIG. 1, the hydrogenatedproduct 52 may be further processed in a fuel composition separationunit 60, removing any remaining byproducts from the hydrogenated product52, such as hydrogen gas, water, C₂-C₉ hydrocarbons, or C₁₅₊hydrocarbons, thereby producing a targeted fuel composition. The fuelcomposition separation unit 60 may comprise a number of distillationtowers. In some embodiments, the various composition streams areseparated using at least four distillation towers. In other embodiments,three towers or less are used to separate the fuel compositions.

In one embodiment, the hydrogenated product 52 may be separated into thedesired fuel C₉-C₁₅ product 64, and a light-ends C₂-C₉ fraction 62and/or a C₁₅₊ heavy-ends fraction 66. Distillation may be used toseparate the fractions. Alternatively, in other embodiments, such as fora naphtha- or kerosene-type jet fuel composition, the heavy endsfraction 66 can be separated from the desired fuel product 64 by coolingthe hydrogenated product 52 to approximately −40° C., −47° C., or −65°C. and then removing the solid, heavy ends fraction 66 by techniquesknown in the art such as filtration, decantation, or centrifugation.

With regard to the esters 34 from the distillation unit 30, in certainembodiments, the esters 34 may be entirely withdrawn as an ester productstream 36 and processed further or sold for its own value, as shown inFIG. 1. As a non-limiting example, the esters 34 may comprise varioustriglycerides that could be used as a lubricant. Based upon the qualityof separation between olefins and esters, the esters 34 may comprisesome heavier olefin components carried with the triglycerides. In otherembodiments, the esters 34 may be further processed in a biorefinery oranother chemical or fuel processing unit known in the art, therebyproducing various products such as biodiesel or specialty chemicals thathave higher value than that of the triglycerides, for example.Alternatively, in certain embodiments, the esters 34 may be partiallywithdrawn from the system and sold, with the remainder further processedin the biorefinery or another chemical or fuel processing unit known inthe art.

In certain embodiments, the ester stream 34 is sent to atransesterification unit 70. Within the transesterification unit 70, theesters 34 are reacted with at least one alcohol 38 in the presence of atransesterification catalyst. In certain embodiments, the alcoholcomprises methanol and/or ethanol. In another embodiment, the alcohol 38comprises glycerol (and the transesterification reaction is aglycerolysis reaction). In one embodiment, the transesterificationreaction is conducted at approximately 60-70° C. and approximately 1atm. In certain embodiments, the transesterification catalyst is ahomogeneous sodium methoxide catalyst. Varying amounts of catalyst maybe used in the reaction, and, in certain embodiments, thetransesterification catalyst is present in the amount of approximately0.5-1.0 weight % of the esters 34.

In certain embodiments, the transesterification reaction may produce atransesterified product 72 comprising monomer C4-C22, C4-C18, or C10-C18olefin esters. In some embodiments, the transesterified product 72comprises monomer terminal olefin esters having the following structure:

where X is a C₃-C₁₈ saturated or unsaturated alkyl chain, and R is analkyl group. In some embodiments, R is methyl. In certain embodiments,the transesterified product 72 comprises monomer fatty acid estersselected from the group consisting of: pentenoic acid esters, hexenoicacid esters, heptenoic acid esters, octenoic acid esters, nonenoic acidesters, decenoic acid esters, undecenoic acid esters, dodecenoic acidesters, tridecenoic acid esters, tetradecenoic acid esters,pentadecenoic acid esters, hexadecenoic acid esters, heptadecenoic acidesters, octadecenoic acid esters, and mixtures thereof. In otherembodiments, the transesterified product 72 comprises terminal olefinsselected from the group consisting of: 4-pentenoic acid ester,5-hexenoic acid ester, 6-heptenoic acid ester, 7-octenoic acid ester,8-nonenoic acid ester, 9-decenoic acid ester, 10-undecenoic acid ester,11-dodecenoic acid ester, 12-tridecenoic acid ester, 13-tetradecenoicacid ester, 14-pentadecenoic acid ester, 15-hexadecenoic acid ester,16-heptadecenoic acid ester, 17-octadecenoic acid ester, and mixturesthereof. In certain embodiments, the transesterified product 72comprises 9-decenoic acid methyl ester (9-DAME) and/or 9-dodecenoic acidmethyl ester (9-DDAME).

The transesterification reaction may produce transesterified products 72including saturated and/or unsaturated monomer fatty acid methyl esters(“FAME”), glycerin, methanol, and/or free fatty acids. In certainembodiments, the transesterified products 72, or a fraction thereof, maycomprise a source for biodiesel. In certain embodiments, thetransesterified products 72 comprise C₁₀-C₁₅ or C₁₁-C₁₄ esters. Incertain embodiments, the transesterified products 72 comprise 9DAesters, 9UDA esters, and/or 9DDA esters. Non-limiting examples of 9DAesters, 9UDA esters and 9DDA esters include methyl 9-decenoate(“9-DAME”), methyl 9-undecenoate (“9-UDAME”), and methyl 9-dodecenoate(“9-DDAME”), respectively. As a non-limiting example, in atransesterification reaction, a 9DA moiety of a metathesized glycerideis removed from the glycerol backbone to form a 9DA ester.

As discussed above, the types of transesterified products formed arebased upon the reactants entering the metathesis reactor 20. In oneparticular embodiment, C₁₂ methyl esters (9-DDAME) are produceddownstream of the metathesis reaction between 3-hexene and a naturaloil.

In another embodiment, a glycerin alcohol may be used in the reactionwith a glyceride stream. This reaction may produce monoglycerides and/ordiglycerides.

In certain embodiments, the transesterified products 72 from thetransesterification unit 70 can be sent to a liquid-liquid separationunit, wherein the transesterified products 72 (i.e., FAME, free fattyacids, and/or alcohols) are separated from glycerin. Additionally, incertain embodiments, the glycerin byproduct stream may be furtherprocessed in a secondary separation unit, wherein the glycerin isremoved and any remaining alcohols are recycled back to thetransesterification unit 70 for further processing.

In one embodiment, the transesterified products 72 are further processedin a water-washing unit. In this unit, the transesterified productsundergo a liquid-liquid extraction when washed with water. Excessalcohol, water, and glycerin are removed from the transesterifiedproducts 72. In another embodiment, the water-washing step is followedby a drying unit in which excess water is further removed from thedesired mixture of esters (i.e., specialty chemicals). Such specialtychemicals include non-limiting examples such as 9DA, 9UDA, and/or 9DDA,alkali metal salts and alkaline earth metal salts of the preceding,individually or in combinations thereof.

In one embodiment, the monomer specialty chemical (e.g., 9DA) may befurther processed in an oligomerization reaction to form a lactone,which may serve as a precursor to a surfactant.

In certain embodiments, the transesterifed products 72 from thetransesterification unit 70 or specialty chemicals from thewater-washing unit or drying unit are sent to an ester distillationcolumn 80 for further separation of various individual or groups ofcompounds, as shown in FIG. 1. This separation may include, but is notlimited to, the separation of 9DA esters, 9UDA esters, and/or 9DDAesters. In one embodiment, the 9DA ester 82 may be distilled orindividually separated from the remaining mixture 84 of transesterifiedproducts or specialty chemicals. In certain process conditions, the 9DAester 82 should be the lightest component in the transesterified productor specialty chemical stream, and come out at the top of the esterdistillation column 80. In another embodiment, the remaining mixture 84,or heavier components, of the transesterified products or specialtychemicals may be separated off the bottom end of the column. In certainembodiments, this bottoms stream 84 may potentially be sold asbiodiesel.

The 9DA esters, 9UDA esters, and/or 9DDA esters may be further processedafter the distillation step in the ester distillation column. In oneembodiment, under known operating conditions, the 9DA ester, 9UDA ester,and/or 9DDA ester may then undergo a hydrolysis reaction with water toform 9DA, 9UDA, and/or 9DDA, alkali metal salts and alkaline earth metalsalts of the preceding, individually or in combinations thereof.

In certain embodiments, the monomer fatty acid esters from thetransesterified products 72 may be reacted with each other to form otherspecialty chemicals such as dimers.

In other embodiments, specific ester products, such as 9DDA methylester, may be enriched through subsequent processing and reaction stepsof the transesterified products. In one embodiment, a C₁₀ methyl esterstream may be separated from heavier C₁₂₊ methyl esters. The C₁₀ methylester stream may then be reacted with 1-butene in the presence of ametathesis catalyst to form C₁₂ methyl esters and ethylene. The ethylenemay be separated from the methyl esters and the C10 and C12 methylesters may be removed or returned to an ester distillation column forfurther processing.

In certain embodiments, the monomer fatty acids and/or monomer fattyacid esters from the transesterified products 72 are isomerized to formisomerized monomer fatty acids and/or isomerized monomer fatty acidesters. Through the isomerization reaction of the unsaturated fatty acidor fatty acid ester, the olefinic double bond can migrate to severalpositions on the carbon chain. For example, isomerization of 9-DAME canproduce a mixture of products such as x-DAME, wherein x is 3-9.Isomerization of 9-DDAME can lead to x-DDAME, wherein x is 3-11. Theseisomeric mixtures may perform better as surfactants because lower CMC(critical micelle concentration) values are attainable. Isomerizationmay also reduce the melting point of the starting olefinic compositionby at least 5° C., 10° C., 15° C., or 20° C. In other embodiments,isomerization may increase the solubility of the composition at ambienttemperature (i.e., 20-25° C.) by at least 5%, 10%, 15%, 20%, or 25%. Inother words, the isomerizated composition may have a solubility that isat least 5%, 10%, 15%, 20%, or 25% higher than the solubility of thestarting olefinic composition. In some embodiments, isomerization mayincrease the solubility at approximately 0° C. by at least 5%, 10%, or15%.

The isomerization of the fatty acids and/or fatty acid esters from thetransesterified products 72 may be conducted at an elevated temperature(i.e., greater than 25° C.). In certain embodiments, the temperature ofthe heat treatment for the isomerization reaction is greater than 100°C., greater than 150° C., or greater than 200° C. In other embodiments,the temperature is between 100° C.-300° C., between 150-250° C., orabout 200° C. In some embodiments, the heat treatment step is conductedin the presence of an isomerization catalyst. Examples of the varioustypes of isomerization catalysts are discussed above.

In certain embodiments, the monomer fatty acids and/or monomer fattyacid esters that undergo the isomerization reaction are selected fromthe group consisting of: 9DA, 9DA esters, 9UDA, 9UDA esters, 9DDA, and9DDA esters. The isomerization of the fatty acids and/or fatty acidesters may produce isomerized monomer fatty acids and/or isomerizedmonomer fatty acid esters selected from the group consisting ofisomerized 9DA, isomerized 9DA esters, isomerized 9UDA, isomerized 9UDAesters, isomerized 9DDA, and isomerized 9DDA esters.

Isomerizing the monomer fatty acids and/or monomer fatty acid esters mayimprove various performance properties. For example, the isomericmixtures may perform better as surfactants because lower CMC (criticalmicelle concentration) values are attainable. Further, the isomerizedproduct composition may have an observed broadening of the freezing andmelting points, which may allow for transportation of the isomerizedfatty acid/ester product composition at higher concentrations of themonomer fatty acids and/or monomer fatty acid esters without incurringshipping problems. In some embodiments, isomerization may reduce themelting point of the starting olefinic composition by at least 5° C.,10° C., 15° C., or 20° C. In other embodiments, isomerization mayincrease the solubility of the composition at ambient temperature (i.e.,20-25° C.) by at least 5%, 10%, 15%, 20%, or 25%. In other words, theisomerizated composition may have a solubility that is at least 5%, 10%,15%, 20%, or 25% higher than the solubility of the starting olefiniccomposition. In some embodiments, isomerization may increase thesolubility at approximately 0° C. by at least 5%, 10%, or 15%.

Isomerized monomer fatty acids and/or isomerized monomer fatty acidesters may be used in a variety of different commercial applications,including, but not limited to: lubricants, waxes, films, paints, paintstrippers, coatings, plasticizers, resins, binders, solvents, polyols,soil stabilization, chemical grouting, oilfield drilling fluids, cropprotection products, surfactants, intermediates, and adhesives.

In certain embodiments, the transesterified product 72 comprisesterminal olefin esters and is cross-metathesized with an internal olefinin the presence of a metathesis catalyst to produce a dibasic acidand/or dibasic ester, as well as an olefin byproduct. As mentionedabove, the transesterified product 72 may comprise terminal olefinshaving the following structure:

where X is a C₃-C₁₈ saturated or unsaturated alkyl chain, and R is analkyl group or hydrogen.

In certain embodiments, the terminal olefin-internal olefincross-metathesis reaction is conducted at a weight ratio between 1:99(terminal to internal) and 99:1 (terminal to internal). In otherembodiments, the weight ratio of the terminal and internal olefin isbetween 1:5 and 5:1. In yet other embodiments, the weight ratio betweenthe terminal and internal olefin is between 1:2 and 2:1. In oneparticular embodiment, the weight ratio between the terminal andinternal olefin is approximately 1:1.

In certain embodiments, the terminal olefin is selected from the groupconsisting of: 4-pentenoic acid ester, 5-hexenoic acid ester,6-heptenoic acid ester, 7-octenoic acid ester, 8-nonenoic acid ester,9-decenoic acid ester, 10-undecenoic acid ester, 11-dodecenoic acidester, 12-tridecenoic acid ester, 13-tetradecenoic acid ester,14-pentadecenoic acid ester, 15-hexadecenoic acid ester,16-heptadecenoic acid ester, 17-octadecenoic acid ester, acids thereof,and mixtures thereof. In one particular embodiment, the terminal olefinis 9-decenoic acid ester.

In certain embodiments, the terminal olefin is cross-metathesized withan internal olefin selected from the group consisting of: pentenoic acidesters, hexenoic acid esters, heptenoic acid esters, octenoic acidesters, nonenoic acid esters, decenoic acid esters, undecenoic acidesters, dodecenoic acid esters, tridecenoic acid esters, tetradecenoicacid esters, pentadecenoic acid esters, hexadecenoic acid esters,heptadecenoic acid esters, octadecenoic acid esters, acids thereof, andmixtures thereof. In one particular embodiment, the internal olefin is9-undecenoic acid ester. In another particular embodiment, the internalolefin is 9-dodecenoic acid ester.

In some embodiments, the internal olefin is formed by reacting a portionof the terminal olefin ester derived from the transesterified product 72with a low-molecular-weight internal olefin or mid-weight internalolefin in the presence of a metathesis catalyst. In certain embodiments,the low-molecular-weight internal olefin is selected from the groupconsisting of: 2-butene, 2-pentene, 2-hexene, 3-hexene, 2-heptene,3-heptene, 2-octene, 3-octene, 4-octene, 2-nonene, 3-nonene, 4-nonene,and mixtures thereof. In one particular embodiment, thelow-molecular-weight internal olefin is 2-butene. In another particularembodiment, the low-molecular-weight internal olefin is 3-hexene.

In certain embodiments, at least 70 wt %, 80 wt %, or 90 wt % dibasicester and/or dibasic acid is formed from the cross-metathesis reactionof a terminal olefin and an internal olefin in the presence of less than150 ppm, 100 ppm, 50 ppm, 25 ppm, or ppm catalyst. A comparableself-metathesis reaction with terminal olefins (such as 9-decenoic acidester) under similar reaction conditions may require more catalyst(e.g., more than 150 ppm, or more than 500 ppm) to achieve similaryields of dibasic esters and/or dibasic acids (potentially due to theformation of the ethylene byproduct).

In certain embodiments, the dibasic ester and/or dibasic acid yield isimproved by separating the olefin byproduct formed in thecross-metathesis reaction from the metathesis product while the reactionbetween the terminal olefin and internal olefin is ongoing. In otherembodiments, the dibasic ester and/or dibasic acid yield is improved bysparging the metathesis products in the metathesis reactor with achemically inert gas (e.g., nitrogen, argon, or helium) to ventilatedissolved gases/byproducts (e.g., olefin byproducts) in the metathesisproduct.

In certain embodiments, the cross-metathesis reaction of the terminalolefin and internal olefin produces a dibasic ester comprising thefollowing structure:

wherein R and R′ are independently alkyl or aryl groups, and Y is anolefin comprising between 6 and 36 carbon atoms. In some embodiments,the cross-metathesis reaction forms a C₂₁-C₂₄ dibasic ester. In oneembodiment, the cross-metathesis reaction forms a dibasic ester, where Rand R′ are methyl and Y is 8-hexadecene (i.e., the dibasic ester formedfrom the cross-metathesis reaction of a terminal olefin and an internalolefin is dimethyl 9-octadecenedioate).

In some embodiments, the dibasic ester derived from the transesterifiedproduct 72 may further undergo a hydrolysis reaction with water to forma dibasic acid having the following structure:

wherein Y is an olefin comprising between 6 and 36 carbon atoms. In oneembodiment, Y is 8-hexadecene (i.e., the dibasic acid is 9-octadecenedioic acid).

Following hydrolysis, in some embodiments, the product stream may besent to a flash column or decanter to remove methanol and water from thediacid.

In other embodiments, the dibasic acid and/or dibasic ester isisomerized to form an isomerized dibasic acid and/or isomerized dibasicester. The isomerization of the dibasic acid and/or dibasic ester may beconducted at an elevated temperature (i.e., greater than 25° C.). Incertain embodiments, the temperature of the heat treatment for theisomerization reaction is greater than 100° C., greater than 150° C., orgreater than 200° C. In other embodiments, the temperature is between100° C.-300° C., between 150-250° C., or about 200° C. In someembodiments, the heat treatment step is conducted in the presence of anisomerization catalyst. Examples of the various types of isomerizationcatalysts are discussed above.

In certain embodiments, the isomerized dibasic acid and/or isomerizeddibasic ester comprises compounds selected from the group consisting of:isomerized dimethyl 9-octadecenedioate or isomerized 9-octadecene dioicacid.

In certain embodiments, the isomerized dibasic acid and/or isomerizeddibasic ester is self-metathesized or cross-metathesized with alow-molecular-weight olefin or mid-weight olefin. Typical metathesisreaction conditions and catalysts are discussed in greater detail below.In one embodiment, the isomerized dibasic acid and/or isomerized dibasicester is self-metathesized in the presence of approximately 10 ppm, 20ppm, 40 ppm, 50 ppm, 80 ppm, 100 ppm, 120 ppm, or greater than 150 ppmmetathesis catalyst.

In certain embodiments, the isomerized fatty acid, isomerized fatty acidester, dibasic acid, dibasic ester, isomerized dibasic acid, and/orisomerized dibasic ester is hydrogenated. Typical hydrogenation reactionconditions and catalysts are discussed above. In one particular example,the hydrogenation reaction is conducted in the presence of a nickelbased catalyst at approximately 150° C. and 150 psig.

As noted, the self-metathesis of the natural oil, cross-metathesisbetween the natural oil and low-molecular-weight olefin or mid-weightolefin, or cross-metathesis between a terminal olefin and internalolefin occurs in the presence of a metathesis catalyst. As statedpreviously, the term “metathesis catalyst” includes any catalyst orcatalyst system that catalyzes a metathesis reaction. Any known orfuture-developed metathesis catalyst may be used, individually or incombination with one or more additional catalysts. Non-limitingexemplary metathesis catalysts and process conditions are described inPCT/US2008/009635, pp. 18-47, incorporated by reference herein. A numberof the metathesis catalysts as shown are manufactured by Materia, Inc.(Pasadena, Calif.).

The metathesis process can be conducted under any conditions adequate toproduce the desired metathesis products. For example, stoichiometry,atmosphere, solvent, temperature, and pressure can be selected by oneskilled in the art to produce a desired product and to minimizeundesirable byproducts. The metathesis process may be conducted under aninert atmosphere. Similarly, if a reagent is supplied as a gas, an inertgaseous diluent can be used. The inert atmosphere or inert gaseousdiluent typically is an inert gas, meaning that the gas does notinteract with the metathesis catalyst to substantially impede catalysis.For example, particular inert gases are selected from the groupconsisting of helium, neon, argon, nitrogen, individually or incombinations thereof.

In certain embodiments, the metathesis catalyst is dissolved in asolvent prior to conducting the metathesis reaction. In certainembodiments, the solvent chosen may be selected to be substantiallyinert with respect to the metathesis catalyst. For example,substantially inert solvents include, without limitation, aromatichydrocarbons, such as benzene, toluene, xylenes, etc.; halogenatedaromatic hydrocarbons, such as chlorobenzene and dichlorobenzene;aliphatic solvents, including pentane, hexane, heptane, cyclohexane,etc.; and chlorinated alkanes, such as dichloromethane, chloroform,dichloroethane, etc. In one particular embodiment, the solvent comprisestoluene.

In other embodiments, the metathesis catalyst is not dissolved in asolvent prior to conducting the metathesis reaction. The catalyst,instead, may be slurried with the natural oil 12, where the natural oil12 is in a liquid state. Under these conditions, it is possible toeliminate the solvent (e.g., toluene) from the process and eliminatedownstream olefin losses when separating the solvent. In otherembodiments, the metathesis catalyst may be added in solid state form(and not slurried) to the natural oil 12 (e.g., as an auger feed).

The metathesis reaction temperature may be a rate-controlling variablewhere the temperature is selected to provide a desired product at anacceptable rate. In certain embodiments, the metathesis reactiontemperature is greater than about −40° C., greater than about −20° C.,greater than about 0° C., or greater than about 10° C. In certainembodiments, the metathesis reaction temperature is less than about 150°C., or less than about 120° C. In one embodiment, the metathesisreaction temperature is between about 10° C. and about 120° C.

The metathesis reaction can be run under any desired pressure.Typically, it will be desirable to maintain a total pressure that ishigh enough to keep the cross-metathesis reagent in solution. Therefore,as the molecular weight of the cross-metathesis reagent increases, thelower pressure range typically decreases since the boiling point of thecross-metathesis reagent increases. The total pressure may be selectedto be greater than about 0.1 atm (10 kPa), in some embodiments greaterthan about 0.3 atm (30 kPa), or greater than about 1 atm (100 kPa).Typically, the reaction pressure is no more than about 70 atm (7000kPa), in some embodiments no more than about 30 atm (3000 kPa). Anon-limiting exemplary pressure range for the metathesis reaction isfrom about 1 atm (100 kPa) to about 30 atm (3000 kPa).

While the invention as described may have modifications and alternativeforms, various embodiments thereof have been described in detail. Itshould be understood, however, that the description herein of thesevarious embodiments is not intended to limit the invention, but on thecontrary, the intention is to cover all modifications, equivalents, andalternatives falling within the spirit and scope of the invention asdefined by the claims. Further, while the invention will also bedescribed with reference to the following non-limiting examples, it willbe understood, of course, that the invention is not limited theretosince modifications may be made by those skilled in the art,particularly in light of the foregoing teachings.

EXAMPLES Example 1

A clean, dry, stainless steel jacketed 5-gal. Parr reactor vesselequipped with a dip tube, overhead stirrer, internal cooling/heatedcoils, temperature probe, sampling valve, and headspace gas releasevalve was purged with argon to 15 psig. Soybean oil (SBO, 2.5 kg, 2.9mol, Costco, MWn=864.4 g/mol, 85 weight % unsaturation as determined bygas chromatographic analysis (“by gc”), 1 hour argon sparged in 5-galcontainer) was added into the Parr reactor. The Parr reactor was sealedand the SBO was purged with argon for 2 hours while cooling to 10° C.After 2 hours, the reactor was vented until the internal pressurereached 10 psig. The dip tube valve on the reactor was connected to a1-butene cylinder (Airgas, CP grade, 33 psig headspace pressure, >99weight %) and re-pressurized to 15 psig of 1-butene. The reactor wasvented again to 10 psig to remove residual argon in the headspace. TheSBO was stirred at 350 rpm and 9-15° C. under 18-28 psig 1-butene until3 mol 1-butene per SBO olefin bond was transferred into the reactor(approximately 2.2 kg 1-butene over approximately 4-5 hours). A toluenesolution of[1,3-Bis-(2,4,6-trimethylphenyl)-2-imidazolidinylidene]dichlororuthenium(3-methyl-2-butenylidene)(tricyclohexylphosphine)(C827, Materia) was prepared in Fischer-Porter pressure vessel bydissolving 130 mg catalyst in 30 grams of toluene as a catalyst carrier(10 mol ppm per olefin bond of SBO) and was added to the reactor via thereactor dip tube by pressurizing the headspace inside the Fischer-Portervessel to 50-60 psig with argon. The Fischer-Porter vessel and dip tubewere rinsed with an additional 30 g toluene. The reaction mixture wasstirred for 2.0 hours at 60° C. The reaction mixture was allowed to coolto ambient temperature while the gases in the headspace were vented.After the pressure was released, the reaction mixture was transferred toa 3-neck round bottom flask containing 58 g bleaching clay (2% w/w SBO,Pure Flow B80 CG) and a magnetic stir bar. The reaction mixture wastreated by stirring at 85° C. under argon. After 2 hours, during whichtime any remaining 1-butene was allowed to vent, the reaction mixturewas allowed to cool to 40° C. and filtered through a fritted glassfilter. An aliquot of the product mixture was found by gaschromatographic analysis (following transesterification with 1% w/wNaOMe in methanol at 60° C.) to contain approximately 22 weight % methyl9-decenoate, approximately 16 weight % methyl 9-dodecenoate,approximately 3 weight % dimethyl 9-octadecenedioate, and approximately3 weight % methyl 9-octadecenoate (by gc). These results comparefavorably with the calculated yields at equilibrium of 23.4 wt % methyl9-decenoate, 17.9 wt % methyl 9-dodecenoate, 3.7 wt % dimethyl9-octadecenedioate, and 1.8 wt % methyl 9-octadecenoate.

Example 2

By the general procedures described in example 1, a reaction wasperformed using 1.73 kg SBO and 3 mol 1-butene/SBO double bond. Analiquot of the product mixture was found by gas chromatographic analysisfollowing transesterification with 1% w/w NaOMe in methanol at 60° C. tocontain approximately 24 weight % methyl 9-decenoate, approximately 18weight % methyl 9-dodecenoate, approximately 2 weight % dimethyl9-octadecenedioate, and approximately 2 weight % methyl 9-octadecenoate(as determined by gc).

Example 3

By the general procedures described in example 1, a reaction wasperformed using 1.75 kg SBO and 3 mol 1-butene/SBO double bond. Analiquot of the product mixture was found by gas chromatographic analysisfollowing transesterification with 1% w/w NaOMe in methanol at 60° C. tocontain approximately 24 weight % methyl 9-decenoate, approximately 17weight % methyl 9-dodecenoate, approximately 3 weight % dimethyl9-octadecenedioate, and approximately 2 weight % methyl 9-octadecenoate(as determined by gc).

Example 4

By the general procedures described in example 1, a reaction wasperformed using 2.2 kg SBO, 3 mol 1-butene/SBO double bond, and the 60 gof toluene used to transfer the catalyst was replaced with SBO. Analiquot of the product mixture was found by gas chromatographic analysisfollowing transesterification with 1% w/w NaOMe in methanol at 60° C. tocontain approximately 25 weight % methyl 9-decenoate, approximately 18weight % methyl 9-dodecenoate, approximately 3 weight % dimethyl9-octadecenedioate, and approximately 1 weight % methyl 9-octadecenoate(as determined by gc).

Example 5

A 12-liter, 3-neck, glass round bottom flask that was equipped with amagnetic stir bar, heating mantle, and temperature controller wascharged with 8.42 kg of the combined reaction products from examples1-4. A cooling condenser with a vacuum inlet was attached to the middleneck of the flask and a receiving flask was connected to the condenser.Hydrocarbon olefins were removed from the reaction product by vacuumdistillation over the follow range of conditions: 22-130° C. pottemperature, 19-70° C. distillation head temperature, and 2000-160 μtorrpressure. The weight of material remaining after the volatilehydrocarbons were removed was 5.34 kg. An aliquot of the non-volatileproduct mixture was found by gas chromatographic analysis followingtransesterification with 1% w/w NaOMe in methanol at 60° C. to containapproximately 32 weight % methyl 9-decenoate, approximately 23 weightmethyl 9-dodecenoate, approximately 4 weight % dimethyl9-octadecenedioate, and approximately 5 weight % methyl 9-octadecenoate(as determined by gc).

Example 6

A 12-liter, 3-neck round bottom flask that was fitted with a magneticstir bar, condenser, heating mantle, temperature probe, and gas adapterwas charged with 4 liters of 1% w/w NaOMe in MeOH and 5.34 kg of thenon-volatile product mixture produced in example 5. The resulting lightyellow heterogeneous mixture was stirred at 60° C. After about an hour,the mixture turned a homogeneous orange color (detected pH=11.) After atotal reaction time of 2 hours, the mixture was cooled to ambienttemperature and two layers were observed. The organic phase was washedtwice with 3 L of 50% (v/v) aqueous MeOH, separated, and neutralized bywashing with glacial HOAc in MeOH (1 mol HOAc/mol NaOMe) to a detectedpH of 6.5, yielding 5.03 kg.

Example 7

A glass, 12 L, 3-neck round bottom flask fitted with a magnetic stirrer,packed column, and temperature controller was charged with the methylester mixture (5.03 kg) produced in example 6 and placed in the heatingmantle. The column attached to the flask was a 2-inch×36-inch glasscolumn containing 0.16″ Pro-Pak™ stainless steel saddles. Thedistillation column was attached to a fractional distillation head towhich a 1 L pre-weighed round bottom flask was fitted for collecting thedistillation fractions. The distillation was carried out under vacuum at100-120 ptorr. A reflux ratio of 1:3 was used for isolating both methyl9-decenoate (9-DAME) and methyl 9-dodecenoate (9-DDAME). A reflux ratioof 1:3 referred to 1 drop collected for every 3 drops sent back to thedistillation column. The samples collected during the distillation, thevacuum distillation conditions, and the 9-DAME and 9-DDAME content ofthe fractions, as determined by gc, are shown in Table 1. Combiningfractions 2-7 yielded 1.46 kg methyl 9-decenoate with 99.7% purity.After collecting fraction 16, 2.50 kg of material remained in thedistillation pot: it was found by gc to contain approximately 14 weight% 9-DDAME, approximately 42 weight % methyl palmitate, and approximately12 weight % methyl stearate.

TABLE 1 Head Pot Distillation temp. temp. Vacuum Weight 9-DAME 9-DDAMEFractions # (° C.) (° C.) (μtorr) (g) (wt %) (wt %) 1 40-47 104-106 1106.8 80 0 2 45-46 106 110 32.4 99 0 3 47-48 105-110 120 223.6 99 0 449-50 110-112 120 283 99 0 5 50 106 110 555 99 0 6 50 108 110 264 99 0 750 112 110 171 99 0 8 51 114 110 76 97 1 9 65-70 126-128 110 87 47 23 1074 130-131 110 64 0 75 11 75 133 110 52.3 0 74 12 76 135-136 110 38 0 7913 76 136-138 100 52.4 0 90 14 76 138-139 100 25.5 0 85 15 76-77 140 110123 0 98 16 78 140 100 426 0 100

Example 8

A reaction was performed by the general procedures described in example1 with the following changes: 2.2 kg SBO, 7 mol propene/mol SBO doublebond, and 200 mg[1,3-Bis-(2,4,6-trimethylphenyl)-2-imidazolidinylidene]dichlororuthenium(benzylidene)(tricyclohexyl-phosphine)[C848 catalyst, Materia Inc., Pasadena, Calif., USA, 90 ppm (w/w) vs.SBO] at a reaction temperature of 40° C. were used. The catalyst removalstep using bleaching clay also was replaced by the following: afterventing excess propene, the reaction mixture was transferred into a3-neck round bottom flask to which 50 mol oftris(hydroxymethyl)phosphine (THMP)/mol C848 catalyst was added. TheTHMP was formed as a 1.0 M solution in isopropanol, where phosphoniumsalt, inorganic salt, formaldehyde, THMPO, and THMP were mixed together.The resulting hazy yellow mixture was stirred for 20 hours at 60° C.,transferred to a 6-L separatory funnel and extracted with 2×2.5 Ldeionized H₂O. The organic layer was separated and dried over anhydrousNa₂SO₄ for 4 hours, then filtered through a fritted glass filtercontaining a bed of silica gel.

Example 9

A reaction was performed by the general procedures described in example8, except that 3.6 kg SBO and 320 mg C848 catalyst were used. Followingcatalyst removal, the reaction product from example 9 was combined withthat from example 8, yielding 5.12 kg of material. An aliquot of thecombined product mixture was found by gas chromatographic analysisfollowing transesterification with 1% w/w NaOMe in methanol at 60° C. tocontain approximately 34 weight % methyl 9-decenoate, approximately 13weight % methyl 9-undecenoate, <1 weight % dimethyl 9-octadecenedioate,and <1 weight % methyl 9-octadecenoate (as determined by gc).

Hydrocarbon olefins were removed from the 5.12 kg of combined reactionproduct described above by vacuum distillation by the general proceduredescribed in example 5. The weight of material remaining after thevolatile olefins were removed was 4.0 kg. An aliquot of the non-volatileproduct mixture was found by gas chromatographic analysis followingtransesterification with 1% w/w NaOMe in methanol at 60° C. to containapproximately 46 weight % methyl 9-decenoate, approximately 18 weight %methyl 9-undecenoate, approximately 2 weight % dimethyl9-octadecenedioate, and approximately 1 weight % methyl 9-octadecenoate(as determined by gc).

Example 10

Two reactions were performed by the general procedures described inexample 8, except that for each reaction, 3.1 kg SBO and 280 mg C848catalyst were used. Following catalyst removal, the reaction productsfrom the two preparations were combined, yielding 5.28 kg of material.An aliquot of the combined product mixture was found by gaschromatographic analysis following transesterification with 1% w/w NaOMein methanol at 60° C. to contain approximately 40 weight % methyl9-decenoate, approximately 13 weight % methyl 9-undecenoate,approximately 2 weight % dimethyl 9-octadecenedioate, and approximately1 weight % methyl 9-octadecenoate (as determined by gc).

Hydrocarbon olefins were removed from the 5.28 kg of combined reactionproduct by vacuum distillation by the general procedure described inexample 5. The weight of material remaining after the volatile olefinswere removed was 4.02 kg. An aliquot of the non-volatile product mixturewas found by gas chromatographic analysis following transesterificationwith 1% w/w NaOMe in methanol at 60° C. to contain approximately 49weight % methyl 9-decenoate, approximately 16 weight % methyl9-undecenoate, approximately 2 weight % dimethyl 9-octadecenedioate, andapproximately 3 weight % methyl 9-octadecenoate (as determined by gc).

Example 11

By the general procedures described in example 10, two metathesisreactions were performed using SBO, 7 mol cis-2-butene/mol SBO doublebond, and 220 mg C848 catalyst/kg SBO. Following catalyst removal, thereaction products from the two preparations were combined, yielding 12.2kg of material. An aliquot of the combined product mixture was found bygas chromatographic analysis following transesterification with 1% w/wNaOMe in methanol at 60° C. to contain approximately 49 weight % methyl9-undecenoate, approximately 2 weight % dimethyl 9-octadecenedioate, andapproximately 1 weight % methyl 9-octadecenoate (as determined by gc).

Hydrocarbon olefins were removed from the 12.2 kg of combined reactionproduct by vacuum distillation by the general procedure described inexample 5. The weight of material remaining after the volatile olefinswere removed was 7.0 kg. An aliquot of the non-volatile product mixturewas found by gas chromatographic analysis following transesterificationwith 1% w/w NaOMe in methanol at 60° C. to contain approximately 57weight % methyl 9-undecenoate, approximately 4 weight % dimethyl9-octadecenedioate, and approximately 2 weight % methyl 9-octadecenoate(as determined by gc).

Example 12

By the general procedures described in example 1, approximately 7 kg ofcross metathesis product was produced by reacting SBO with 3 mol1-butene/mol SBO double bond using 43 mg C827 catalyst/kg SBO, followingcatalyst removal with THMP. An initial 2.09 kg portion of the metathesisproduct was hydrogenated at 136° C. and 400 psig H₂ until hydrogenuptake ceased in a one gallon batch autoclave using 105 g ofJohnson-Matthey A-7000 Sponge Metal™ catalyst. The resulting mixture wasfiltered warm (22-55° C.), yielding 1.40 kg filtrate and 350 g of amixture consisting of the catalyst and the hydrogenated product. Theentirety of the catalyst-containing mixture was returned to the onegallon reactor along with a second 2.18 kg portion of the metathesisproduct and a second hydrogenation reaction was similarly carried outuntil hydrogen uptake ceased. The catalyst was allowed to settle and themajority of the organic product was decanted and filtered, yielding 1.99kg filtrate and 380 g catalyst-hydrogenated product mixture. Theremaining approximately 3 kg of metathesis product was hydrogenated intwo additional batch reactions that in like manner were carried outusing the catalyst from the previous reaction, yielding 1.65 kg and 1.28kg of hydrogenated product, respectively. The total weight ofhydrogenated product that was isolated after filtration was 6.32 kg.Aliquots of the hydrogenated product were found by gas chromatographicanalysis to contain approximately 30 weight % C₆-C₁₈ n-paraffins andapproximately 70 weight % triglycerides. The relative distribution ofthe C₈-C₁₈ n-paraffins contained in the hydrogenated product compareswell with the calculated distribution of olefins by carbon number:observed (calculated) 2.3 (0.6) weight % C₈, 35.6 (36.2) weight % C₉,30.0 (27.6) weight % C₁₀, 0.6 (0.1) weight % C₁₁, 22.2 (23.6) weight %C₁₂, 3.4 (3.7) weight % C₁₃, 0.1 (0.0) weight % C₁₄, 4.4 (6.3) weight %C₁₅, 0.4 (0.4) weight % C₁₆, 0.1 (0.0) weight % C₁₇, and 1.0 (1.6)weight % C₁₈. The paraffin components were separated by wiped filmevaporation from a 4.84 kg aliquot of the hydrogenatedparaffin/triglyceride product. An initial wiped film evaporation wascarried out at 75° C., 100 torr, 300 rpm, and condensation temperatureof 15° C. using a feed rate of 300 g/h and yielded a condensate that wassubjected to a second wiped film evaporation at 125° C., 90 torr, 300rpm, and condensation temperature of 10° C. to remove the lighteralkanes. The resultant residual liquid was found by gas chromatographyto contain the following distribution of n-alkanes: 17.5 weight % C₇,1.7 weight % C₈, 31.0 weight % C₉, 28.3 weight % C₁₀, 0.6 weight % C₁₁,17.4 weight % C₁₂, 2.1 weight % C₁₃, 0.1 weight % C₁₄, 1.2 weight % C₁₅,0.1 weight % C₁₆, 0.0 weight % C₁₇, and 0.1 weight % C₁₈. The materialwas found to have a heat of combustion of 43.86 MJ/kg (ASTM D3338), lessthan 1 mg/kg sulfur (ASTM D5453), density of 0.7247 (ASTM D4052), and afinal boiling point of 232.3° C. (ASTM D86), indicating the majority ofthis material would be suitable as a blend stock in a fuel applicationsuch as diesel or jet fuel.

Example 13

An oligomerization reaction of 1-olefin/1,4-diene (92 wt % 1-decene, 4.5wt % 1,4-decadiene, 2 wt % 1,4-undecadiene) that was produced from thecross metathesis of palm oil with 1-octene was performed on a 550 gscale using 1.1 mol % ethyl aluminum dichloride (1M solution inhexane)/1.1 mol % tert-butyl chloride for 3 hours at 10° C. The reactionmixture was quenched with water and 1M sodium hydroxide solution andstirred until it became colorless. Hexane (300 ml) was added and mixturewas transferred to a separatory funnel. The organic layer was washedwith water and brine, and then concentrated on a rotary evaporator toremove the hexane. The oligomeric mixture was devolatilized via shortpath vacuum distillation (100° C. and 5 Torr) and the productdistribution was determined to be 97% mixture oligomers by GC/MS. Thedynamic viscosity (Brookfield, #34 spindle, 100 rpm, 22° C.) of thesample is 540 cps. The kinematic viscosity for the sample at 40° C. is232 cSt.

Example 14

An Aspen model was developed to simulate the process of maximizing thepurity of an alpha olefin (i.e., 1-decene) based on the metathesisprocess of using a soybean oil feed and 1-butene feed at molar ratio of3:1. A C₁₀-C₁₈₊ olefin stream (Stream A) was created and separateddownstream from the cross-metathesis reaction of the soybean oil feedand 1-butene feed. The C₁₀-C₁₈₊ olefin stream was thencross-metathesized with ethylene in a fixed bed ethylene metathesisreactor to create an olefin product. The ethylene product was separatedfrom the olefin product and recycled back to the ethylene metathesisreactor. A heavier olefin product stream (i.e., C16-C18+) was alsoseparated from the olefin product to form a final olefin product (StreamB) and the heavier olefin product stream was recycled back to theethylene metathesis reactor. The C₁₀-C₁₈₊ olefin input stream (Stream A)and final olefin product stream (Stream B) have the following olefinproduct distributions, shown in Table 2 below:

TABLE 2 Stream A Stream B Olefin Distribution wt % wt % C10:1 36.1 86.8C10 isomers 52.7 3.0 C11 0.0 0.0 C12 0.0 1.8 C13 0.0 4.1 C14-18 11.2 4.3Total 100.0 100

Example 15

An Aspen model was developed to simulate the process of maximizingheavier weight olefins (i.e., C₁₈₊ olefins) based on the metathesisprocess of using a soybean oil feed and a hexene isomer feed at molarratio of 3:1. A C₁₁-C₁₈₊ olefin stream (Stream A) was created andseparated downstream from the cross-metathesis reaction of the soybeanoil feed and hexene isomer feed. The C₁₁-C₁₈₊ olefin stream was thenself-metathesized in a fixed bed reactor to create an olefin product. AC₁₁-C₁₆ olefin stream was separated from the olefin product recycledback to the self-metathesis reactor. The C₁₀ olefin can also beseparated as a product to form a final olefin product stream (B). Theolefin input stream (Stream A) and final product stream (Stream B) havethe following olefin product distributions, shown in Table 3 below:

TABLE 3 Stream A Stream A Stream B Olefin Distribution wt % wt % <C100.0 2.5 C10 0.0 21.3 C11 24.7 0.0 C12 36.2 0.0 C13 16.8 0.0 C14 4.5 0.0C15 12.1 0.0 C16 2.4 0.0 C17 0.4 4.1 C18 2.4 46.7 C18+ 0.5 25.4 Total100.0 100

Example 16

An Aspen model was developed to simulate the process of maximizing thepurity of C₁₁-C₁₅ methyl esters based on the metathesis process of usinga soybean oil feed and a hexene isomer feed at molar ratio of 3:1. Amixed triglyceride and ester stream is formed from the cross-metathesisreaction of the soybean oil and hexene isomer feeds. The mixedtriglyceride and ester stream undergoes glycerolysis after metathesis,followed by olefin separation and transesterification. A C₁₀ and lighterolefin stream is separated from the mixed triglyceride and ester streamand recycled back to the metathesis reactor. A C₁₀ methyl ester (ME)stream is also recycled to the metathesis reactor. A C₁₆ ME stream ispurged. A fraction (e.g., 10%) of the C₁₇-C₂₀ ME stream is purged andthe remaining fraction, mixed with the heavier esters, is recycled backto the metathesis reactor. The final ester product stream (comprisingprimarily C₁₁-C₁₅ ME) downstream of the olefin separation,transesterification, and ester recycle streams has the following esterdistribution, shown in Table 4:

TABLE 4 Ester Product FAME Stream Distribution wt % <C10ME 0.0 C10ME 0.0C11ME 17.3 C12ME 21.7 C13ME 17.7 C14ME 4.6 C15ME 16.8 C16ME 15.6 C17ME0.1 C18ME 6.2 C18 + ME 0.0 Total 100.0

Example 17 9-DAME/9-DDAME on a 10 g Scale

In this example, methyl 9-decenoate (distillation cut from butenolyzed,stripped, trans-esterified palm oil), and methyl 9-dodecenoate(distillation cut from butenolyzed, stripped, trans-esterified palm oil)were prepared and cross-metathesized. Their compositions are shown inTables 5 and 6 below. PV was undetected (AOCS method AOCS Method Cd8b-90 Peroxide Value Acetic Acid-Isooctane Method (Revised 2003)).

TABLE 5 9-DAME Feed composition Component Wt % 1,4-tridecadiene 0.18Methyl 8-nonenoate 0.08 Methyl decanoate 0.16 Methyl 9-decenoate 98.51Methyl 8-decenoate 0.76 Other 0.29 TOTAL 100.00

TABLE 6 9-DDAME feed composition Component Wt % 6-pentadecene 0.183,6-pentadecadiene 0.21 7-hexadecene 0.25 Methyl decanoate 0.01 Methyl9-decenoate 0.76 Methyl decanoate 3.01 Methyl 9-dodecenoate* 95.46 Other0.12 TOTAL 100.00 *contaminated with 11-isomer dodecenoic acid, methylester

Clean, dry, 20 CC scintillation vials outfitted with a magnetic stir barand septum top were charged with 9-DAME or a mixture of 9-DAME/9-DDAMEaccording to the experiment design Table 7 below.

TABLE 7 C-827 Headspace Example 9-DAME 9-DDAME (ppm wt) Treatment 17a10.02 g 0 g 80 Vent only (comparative) 17b 10.00 g 0 g 80 Nitrogen purge(comparative) 17c 10.00 g 0 g 500 Vent only (comparative) 17d 10.00 g 0g 500 Nitrogen purge (comparative) 17e 4.42 g 5.60 g 80 Vent only 17f4.41 g 5.61 g 80 Nitrogen purge

The vials were placed in an eight-cell aluminum block on top of aheater/stirrer. The aluminum block was heated to 60° C. While thealuminum block was heating (˜15 min.), the vial headspace was degassedby providing a nitrogen inlet (˜65 mL/min) and an exhaust needle.Meanwhile, a metathesis catalyst solution (0.01 mg/μL) was prepared byfirst placing C-827 (21.10 mg) in a 2 mL volumetric flask, secondcapping the flask with a rubber septum, third purging with nitrogen, andfourth adding toluene to the 2.00 mL mark. Metathesis catalyst solutionwas added to each reaction mixture (time=0). According to theexperimental design, the nitrogen inlet (65 mL/min) was left in place tosweep by-product olefins away from the reaction or it was removed. Inboth cases the vent needle was left in place to avoid over-pressuringthe scintillation vial. In the latter case, the oxygen free headspacewas provided by olefin formed by metathesis. After 2 hours, thecomposition (normalized wt %, exclusive of light olefins) was determinedby GC FID2, Table 8.

TABLE 8 17a 17b 17c 17d 17e 17f Methyl 8- 1.39 1.67 3.58 3.65 0.00 0.00nonenoate Methyl 9- 80.51 77.53 41.12 28.66 28.41 17.48 decenoate Methyl8- 0.00 0.00 4.41 4.86 0.00 0.00 decenoate Methyl 0.00 0.00 3.87 3.410.00 0.00 undecenoate Methyl 9- 0.00 0.00 0.00 0.00 29.44 12.59dodecenoate Methyl 9- 0.09 0.10 0.18 0.19 0.35 0.58 octadecenoateDimethyl 0.12 0.17 0.41 0.96 0.00 0.00 hexadecenedioate Dimethyl 0.450.65 5.14 8.63 0.62 1.04 heptadecenedioate Dimethyl 9- 16.25 18.80 39.0846.37 36.28 62.68 octadecenedioate Dimethyl 0.00 0.00 0.50 1.09 0.000.00 nonadecenedioate Dimethyl 0.00 0.00 0.00 0.00 0.89 1.54eicosenedioate Other 1.20 1.08 1.73 2.19 4.00 4.11 Total 100 100 100 100100 100

Example 18 9-DAME/9-DDAME on a 330 g Scale

A dibasic ester composition was produced by conducting across-metathesis reaction between methyl 9-decenoate (9-decenoic acidmethyl ester, 9-DAME) and methyl 9-dodecenoate (9-dodecenoic acid methylester, 9-DDAME). A 1.0:1.0 mole ratio mixture of 9-DAME and 9-DDAME (332g) was charged to a 1 L round bottom flask and heated to 60° C. Pressurewas adjusted to 100 mg Hg with ChemGlass diaphragm vacuum pump modelCG-4812-30/and J-Kem Scientific Digital Vacuum Regulator Model 200 andstirring was initiated with a magnetic stir bar. The feed composition(distillation cut from butenolyzed, stripped, trans-esterified palm oil)is shown below in Table 9.

TABLE 9 Component wt % Methyl decanoate 0.04 Methyl 9-decenoate 44.81Methyl 8-decenoate 0.07 Methyl undecenoate 0.19 Methyl decanoate 0.76Methyl 9-dodecenoate* 52.87 Methyl 9,12-tridecadienoate 0.86 Methyltetradecenoate 0.20 Methyl 9-pentadecenoate 0.03 Methyl9,12-pentadienoate 0.02 Methyl hexadecanoate 0.15 Total 100*contaminated with methyl 11-dodecenoate

After the system stabilized at desired conditions, 80 ppm of C-827 (astoluene solution) was added (t=0 min). At approximately 15-20 min, thereaction started bubbling vigorously and the pressure rose toapproximately 500 mm Hg. Pressure re-stabilized at 100 mm Hg afterapproximately 5-10 more minutes. Samples were taken at 30, 60, 90, 120,150, 180, 240, and 300 minutes. At 180 min, an additional 40 ppm ofC-827 (as toluene solution) was added. FIG. 2 shows 9-DAME & 9-DDAME (wt%) verses reaction time (hr).

The crude product composition ((normalized wt %, exclusive of lightolefins)) at five hours is shown in Table 10 below:

TABLE 10 FAME wt % Methyl decanoate 0.05 Methyl 9-decenoate 6.79 Methyl8-decenoate 0.56 Methyl undecenoate 0.37 Methyl dodecanoate 0.84 Methyl9-dodecenoate* 6.53 Methyl 9,12-tridecadienoate 0.05 Methyltetradecenoate 0.20 Methyl hexadecanoate 0.14 Dimethyl hexadecenedioate0.07 Dimethyl heptadecenedioate 1.11 Dimethyl 9-octadecenedioate 78.92Dimethyl nonadecenedioate 0.45 Dimethyl eicosenedioate 2.85 Dimethyl9,12-heneicosadienedioate 0.53 99.46 *contaminated with methyl11-dodecenoate

Subsequently, the catalyst was deactivated with 25 equivalents THMP toC-827 at 80° C. for 120 min, THMP being prepared by the generalprocedure of example 8. The catalyst was then removed by waterextraction (5:1 oil to water). The composition was dried with MgSO₄.Then, light FAME stripping was conducted at 1 mm Hg and approximately100° C. The wt % concentration of the various products included a largefraction of 18:1 dibasic ester, see Table 11.

TABLE 11 Component Content (wt %) Methyl Hexadecenoate 0.17 Dimethyl8-hexadecenedioate 0.06 Dimethyl 8-heptadecenedioate 1.34 Dimethyl9-octadecenedioate 92.95 Dimethyl nonadecenedioate 0.58 Dimethyleicosenedioate 3.41 Dimethyl 9,12-heneicosadienedioate 0.92 Heavies 0.57

Example 19 9-DAME/9-DDAME on a 3 kg Scale

A 12 L glass round bottom flask fitted with 1) a reflux condenser (5 C)to which a vacuum gauge and ChemGlass diaphragm vacuum pump modelCG-4812-30 where attached, 2) a rubber septum through which nitrogen andcatalyst were introduced, magnetic stir bar, and thermo-couple andalternate vent (in case vacuum pump failed to maintain sub-atmosphericpressure). No vacuum regulator was used for this example. Heating wasprovided by heating mantle.

To the nitrogen-purged 12 L reaction-flask was added low PV 9-DAME (1.34kg) and 9-DDAME (1.68 kg). The condenser was chilled to 5 C with glycol.Under continued flow of nitrogen, the mixture was heated to ˜70 C andthen placed under full vacuum. The first catalyst solution (C-827 intoluene) addition marked the beginning of the reaction (t=0 min).Temperature and pressure were recorded, see Table 12.

TABLE 12 Time Temperature Pressure (min) (deg C.) (mm Hg) 0 73.4 35.0 574.2 30.5 10 74.0 30.7 15 72.8 28.7 20 71.5 28.3 25 70.3 28.4 30 69.928.3 35 72.2 28.4 40 72.3 30.9 45 71.4 65.9 50 71.1 233.0 55 70.0 237.560 69.0 196.0 65 68.4 218.6 70 69.1 215.8 75 68.5 188.5 80 68.2 194.2 8570.1 207.9 90 70.0 185.9 95 68.8 175.6 100 68.6 172.8 105 70.2 172.1 11072.2 169.5 115 71.6 170.1 120 71.1 147.0 125 69.3 140.5 140 70.4 92.1150 69.8 74.1 155 71.0 68.6 160 71.1 64.9 165 70.8 57.5 175 69.6 57.5185 70.9 56.6 195 67.3 54.7 210 63.6 56.4 239 56.0 64.5

Catalyst solution was added in 30 mg increments at 0, 10, 22, 32, 40,60, 76, 97, 110, 120, and 121 minutes. Total catalyst added was 0.33 g(110 ppm). The reaction initiated about 5 minutes after the fifthincrement of catalyst. With each addition of catalyst with exception ofthe last two, an increased rate of bubbling was observed. After 239minutes, heat was turned off and the reaction cooled to ambient. Vacuumwas turned off and the system was backfilled with nitrogen. A total of2.66 kg of liquid product were collected. Its composition, analyzed byliquid sample analysis (normalized wt %) is shown in Table 13.

TABLE 13 Initial Final (wt %) (wt %) Butenes 0.00 0.12 3-hexene 0.000.32 1,4-tridecadiene 0.03 0.00 Pentadecene 0.09 0.00 pentadecadiene0.15 0.00 Methyl 8-nonenoate 0.00 0.13 Methyl 9-decenoate 43.59 8.65Methyl 8-decenoate 0.10 0.00 Methyl undecenoate 0.07 0.74 Methyl9-dodecenoate* 55.78 11.50 Methyl 9,12-tridecadienoate 0.06 0.00 Methyltetradecenoate 0.00 0.19 Methyl 9-pentadecenoate 0.00 0.19 Methyl9,12-pentadienoate 0.00 0.08 Methyl 9-octadecenoate 0.00 0.28 Dimethylhexadecenedioate 0.00 0.16 Dimethyl heptadecenedioate 0.00 2.19 Dimethyl9-octadecenedioate 0.13 72.41 Dimethyl nonadecenedioate 0.00 0.23Dimethyl eicosenedioate 0.00 2.74 other 0.00 0.09 TOTAL 100.00 100.00*contaminated with methyl 11-dodecenoate

Samples of the pump exhaust at were collected at 54 minutes (highestoff-gas rate) and at 239 minutes (end of experiment) and then analyzedon GASPRO column (see Table 14 below). Formation of ethylene is evidenceof 9-DAME self-metathesis. Formation of propylene and 2-butene isevidence of isomerization (for instance 9-DAME to 8-DAME).

TABLE 14 Gas sample analysis (area %, known components) At 54 At 239minutes minutes Ethylene 1.67 0.57 Propylene 1.07 1.84 1-butene 92.1746.46 trans-2-butene 0.08 0.09 cis-2-butene 0.03 0.03 trans-3-hexene2.95 14.99 cis-3-hexene 1.02 2.69 Toluene 0.62 30.15

Example 20 9-DAME/9-DDAME on a 10 kg Scale

A clean, dry, stainless steel jacketed 20 liter Parr reactor vesselequipped with a dip tube, overhead stirrer, internal cooling/heatedcoils, temperature probe, sampling valve, and headspace gas releasevalve was purged with nitrogen. Premixed 9-DAME/9-DDAME feedstock (10.08kg, PV=˜13) was charged to the reactor; see Table 15 for composition.The reaction was purged with nitrogen through the dip tube at 14.2 L/min(0.5 scfm) for 30 minutes while gently stirring the mixture. The reactorwas heated to 200° C. and held for 30 minutes while maintaining anitrogen purge of 14.2 L/min (0.5 scfm) through the dip tube and agentle stir rate. The mixture was cooled to 60° C. and nitrogen flow wasreduced to 5.7 L/min (0.2 scfm) with continued stirring. The stirrer wasturned off and a sample was removed through the sample port. PV wasmeasured and no peroxide detected. GC analysis shown in Table 15. Whilemaintaining gentle stirring and a reactor temperature of 60° C., thereactor pressure was reduced to 100 mm Hg. Catalyst solution (0.33 g ofC827 in 40 g of toluene) was added through the sample port (T=0) (9:26).Pressure was maintained at 100 mm Hg with gentle stirring. The firstsample (1st metathesis sample) was collected at 1 hr. Another charge ofcatalyst solution (0.33 g of C827 in 40 g of toluene) was added at 1.5hr. A second sample (2nd metathesis sample) was collected at 2.25 hr.

TABLE 15 Heat 1 hr 2.25 hr Final Feed treated sample sample ProductMethyl 9-decenoate 43.68 42.78 10.92 8.00 6.32 Methyl 9-dodecenoate*55.50 56.10 10.95 8.56 7.93 Methyl 0.00 0.00 0.00 0.01 0.019,12-tridecadienoate Dimethyl 0.00 0.00 0.05 0.08 0.11 hexadecenedioateDimethyl 0.00 0.00 0.54 1.17 1.79 heptadecenedioate Dimethyl 0.00 0.0069.64 73.43 74.76 9-octadecenedioate Dimethyl 0.00 0.00 0.11 0.25 0.38nonadecenedioate Dimethyl 0.00 0.00 4.95 5.33 5.33 eicosenedioateDimethyl 9,12- 0.00 0.00 0.34 0.24 0.25 heneicosadienedioate Other 0.821.12 2.26 2.93 3.12 Total 100.00 100.00 100.00 100.00 100.00*contaminated with methyl 11-dodecenoate

The reaction was stopped. A total of 2.9 kg of olefins was collected incold-traps. Liquid contents of the 20-liter Parr reactor weretransferred at 60° C. to a 20-liter nitrogen purged glass reactor andthen heated to 80° C. With 567 L/min (20 scfm) of nitrogen flowingthrough the headspace, a 1 M THMP solution (433 g) was added to thereactor and vigorous stirring was provided. After 2 h, the mixture wascooled to 35° C. and the stirrer was turned off. The reactor was allowedto set overnight. The next day, the mixture was reheated and thetemperature was maintained between 50° C. and 55° C. Deionized water(1.8 kg) was added and the two-phase system was vigorously stirred for30 minutes. The stirrer was turned off to let phases separate. Thebottom aqueous phase was removed. Another portion of deionized water(1.8 kg) was added to the reactor. The mixture was stirred well mixed.The stirrer was then turned off to let phases separate. The bottomaqueous phase was removed. The final product (6.29 kg) was removed fromthe reactor and analyzed by GC.

Example 21 9-DAME/3-Hexene on 10 g Scale

9-DAME composition (distillation cut from butenolyzed, stripped,transesterified palm oil) is given in Table 5. Clean, dry, 20 ccscintillation vials outfitted with a magnetic stir bar and septum topwas charged with 9-DAME (PV<1) and 3-hexene (distillation cut of olefinsstripped from butenolyzed palm oil) according to the experiment design,Table 16. Each vial was placed in an eight-cell aluminum block on top ofa heater/stirrer. The aluminum block was heated to 60° C. While thealuminum block was heating (˜15 min), the each vial's headspace wasdegassed by providing a nitrogen inlet (˜65 mL/min) and an exhaustneedle. Meanwhile, a 0.01 mg/μL metathesis catalyst solution wasprepared by first placing C827 (21.10 mg) in a 2 mL volumetric flask,second capping the flask with a rubber septum, third purging withnitrogen, and fourth adding toluene to the 2.00 mL mark. Metathesiscatalyst was added to the reaction mixture (time=0). According to theexperimental design, the nitrogen inlet (65 mL/min) was left in place tosweep by-product olefins away from the reaction or it was removed. Inboth cases the vent needle was left in place. In the latter case, olefinformed by metathesis provided the oxygen-free environment needed by thecatalyst. After 2 hours, an aliquot was analyzed by GC. Composition((normalized wt %, exclusive of light olefins) is shown in Table 17.

TABLE 16 C-827 Example 9-DAME 3-Hexene (ppm wt) Headspace treatment 21a6.42 g 3.61 g 80 Vent only 21b 6.43 g 3.66 g 80 Nitrogen purge 21c 6.42g 3.60 g 120 Vent only 21d 6.44 g 3.58 g 120 Nitrogen purge

TABLE 17 Example 21a 21b 21c 21d Methyl 8-nonenoate 0.00 0.00 0.00 0.00Methyl 9-decenoate 72.85 0.44 10.91 0.46 Methyl 8-decenoate 0.90 0.000.00 0.00 Methyl undecenoate 0.00 0.00 2.17 0.00 Methyl 9-dodecenoate23.24 19.45 58.87 19.34 Methyl tridecenoate 0.00 0.00 0.00 0.00 Methyltetradecenoate 0.00 0.00 0.00 0.00 Methyl 9-octadecenoate 0.00 0.00 0.140.40 Dimethyl hexadecenedioate 0.00 0.00 0.00 0.00 Dimethylheptadecenedioate 0.10 1.75 0.79 1.95 Dimethyl 9-octadecenedioate 1.6874.27 24.48 73.96 Other 1.23 4.09 2.64 3.88 Total 100.00 100.00 100.00100.00

Example 22 9-DAME/Trans-2-Butene on 40 g Scale

9-DAME (40.16 g) was charged to a 100 mL 3-neck round bottom flaskfitted with a coil-type reflux condenser (exhausted to an oil bubbler),a magnetic stir bar, and septum caps. The reaction system was purged,for 30 minutes, with nitrogen by a needle inserted into one of theseptum caps and allowing the exhaust out the bubbler. The reaction flaskwas immersed in an oil batch which was heated to 55° C. The condenserwas cooled by means of 15° C. glycol fluid. Nitrogen purge was replacedby a flow of trans-2-butene through the liquid. After a consistentreflux of trans-2-butene was observed, 80 ppm catalyst was added (T=0).The flow of trans-2-butene was continued for the duration of thereaction except as follows. The reaction was monitored by interruptingtrans-2-butene flow and observing bubble rate in the bubbler. Inaddition to the initial 80 ppm charge of catalyst, three additional 20ppm increments of catalyst were added at T=30, 81, 125 minutes. Finalproduct weight was 31.25 g. Conversion to diesters was 85% andselectivity to 9-ODDAME was 81%.

Example 23 9-DAME/Trans-2-Butene in Fisher-Porter Tube

Using a 3 ounce Fisher-Porter tube equipped with an addition ports forcatalyst and trans-2-butene. In a glove box, 40.0 mg C827 was dissolvedin 1 mL of toluene. Sixty microliters of catalyst solution were loadedinto the catalyst addition manifold using a 250 uL syringe, removed fromglove box, and attached to the pressure vessel manifold. Twenty grams of9-DAME charged to the pressure tube which was subsequently degassed for30 minutes with nitrogen. Meanwhile trans-2-butene wascondensed/transferred into a second 3-ounce Fisher-Porter tube. Thepressure vessel containing trans-2-butene was pressured with nitrogen to4 psig. The pressure vessel containing the ester was heated to 60° C. ina silicone oil bath. The catalyst solution was transferred to the esterunder nitrogen. Immediately, about 7.6 mL (4.57 g) of trans-2-butene(target for 0.75:1 ratio) was transferred to the pressure vesselcontaining the 9-DAME, which washed any residual catalyst solution intothe reaction vessel.

The volume was measured using mm graduation marks on the vessel and themeasured cross sectional area of the tube. The targeted volume was basedon converting the targeted mass to a targeted volume assuming atrans-2-butene density of 0.6 g/mL. The pressure tube containing thereaction mixture was then pressurized to 36 psig with nitrogen. Sampleswere taken at 10 minutes and 60 minutes using a sampling tube apparatus.The vessel was depressurized slowly to atmospheric pressure and spargedwith nitrogen. After 60 minutes of sparging, the vessel wasdisassembled, and the sample was collected. The pressure, bathtemperature, and liquid level were monitored as a function of time andsummarized in Table 18. GC analysis (normalized wt %, exclusive of lightolefins) is summarized in Table 19.

TABLE 18 Time Pressure Temperature Liquid (min) (psig) (° C.) level (mm)Comments 0 36 58.9 60.5 Closed system 5 76 59.2 55.0 Closed system 10 8359.3 55.0 Closed system, Sample #1 10 84 59.2 53.5 Closed system 15 8459.1 53.5 Closed system 20 88 59.1 54.0 Closed system 30 91 58.9 53.5Closed system 40 92 58.9 53.5 Closed system 50 92 58.9 53.5 Closedsystem 60 92 58.9 53.5 Closed system, Sample #2 60 96 58.9 43.5 Nitrogensparge 120 0 Reaction End, Sample #3

TABLE 19 Sample 1 Sample 2 Sample 3 (10 min) (60 min) (120 min) Methyl9-decenoate 36.2 36.9 35.3 Methyl undecenoate 31.9 39.0 39.1 Methyl8-decenoate 2.5 4.3 5.6 Methyl 8-nonenoate 1.3 1.4 1.3 Dimethylhexadecenedioate 0.2 0.1 0.2 Dimethyl heptadecenedioate 2.4 1.8 1.9Dimethyl 9-octadecenedioate 25.4 16.4 16.6 Dimethyl nonadecenedioate 0.10.1 0.1

Example 24 9-DAME/Trans-2-Butene on 8 kg Scale

A two-stage cross-metathesis strategy using 9-DAME and purchasedtrans-2-butene was employed. In the first stage, 9-DAME was partiallyconverted in situ to 9-UDAME. In the second stage, the mixture of 9-DAMEand 9-UDAME was converted to 9-ODDAME. The 9-DAME feedstock (fromoctenolyzed palm oil) for this example was contaminated with significantconcentrations of 8-DAME and 7-tetradecene, Table 20.

TABLE 20 Lot A (wt %) Lot B (wt %) Methyl 9-decanoate 81.4 88.6 Methyl8-decanoate 8.9 5.7 7-tetradecene 8.0 4.6

The two-stage synthesis was performed eight times and was found toscale-up without difficulties. The first batch was performed using aninitial 4 kg charge of an 81% pure 9-DAME and 1.2 mol trans-2-butene/mol9-DAME, yielding a crude product containing 57 wt % 9-ODDAME. The secondpreparation used a 6 kg charge of the 81% pure 9-DAME and only 0.75 moltrans-2-butene/mol 9-DAME, yielding a crude product containing 53 wt %9-ODDAME. The remaining preparations used 8 kg initial charges of 89%pure 9-DAME and 0.75 mol trans-2-butene/mol 9-DAME, yielding crudeproducts containing from 60 to 69 wt % 9-ODDAME. Table 21 summarizes keyreaction measures for the eight batches. Composition is in normalized wt%, exclusive of light olefins.

TABLE 21 Run # 24a 24b 24c 24d 24e 24f 24g 24h 9-DAME lot A A B B B B BB Run size (kg 9-DAME) 4 6 8 8 8 8 8 8 (kg trans-2-butene) 1.4 1.4 1.91.9 1.9 1.9 1.9 1.9 Molar ratio (2-butene : 9-DAME) 1.2 0.75 0.75 0.750.75 0.75 0.75 0.75 C-827 charge (ppmwt) stage 1 93 68 68 68 68 68 68 68stage 2 93 68 68 68 68 68 68 68 Stage 1 wt ratio 9-UDAME : 9-DAME 4.932.43 2.21 2.37 1.88 1.92 1.98 NA Stage 2 composition (wt %) 1-octene0.00 0.00 0.31 0.18 0.31 0.00 0.00 0.00 2-nonene 0.00 2.62 1.09 0.480.68 1.17 0.58 0.46 7-tetradecene 0.75 0.75 0.20 0.18 0.25 0.27 0.110.22 Methyl decanoate 0.35 0.43 0.42 0.41 0.55 0.65 0.69 0.00 Methyl9-decenoate 0.23 1.02 2.08 1.90 2.84 2.20 1.69 1.70 Methyl 8-decenoate0.38 1.71 0.86 0.65 0.91 1.14 0.89 1.04 Methyl undecenoate 2.13 13.6410.38 8.47 11.57 14.00 11.66 11.43 Methyl pentadecenoate 1.39 0.08 0.500.58 0.68 0.77 0.65 0.66 Methyl hexadecenoate 10.30 9.64 5.14 5.83 6.466.96 6.46 6.68 Methyl heptadecenoate 2.08 0.28 0.00 0.00 0.19 0.22 0.190.20 Dimethyl hexadecenedioate 1.19 1.18 0.96 1.11 1.11 1.15 1.12 1.08Dimethyl heptadecenedioate 13.02 12.24 9.26 9.91 9.54 9.42 9.64 9.40Dimethyl 9-octadecenedioate 57.05 53.15 66.79 68.68 64.20 60.34 65.0665.24 Total 97.06 96.74 97.99 98.39 99.28 98.29 98.74 98.10

Purification was accomplished in approximately 2 kg batches bycrystallizing trans-ODDAME from crude product using four volumes of coldmethanol, vacuum filtration including a wash with additional coldmethanol, and then vacuum drying. Typical yield was about 50% andtypical purity is shown in Table 22.

TABLE 22 From lot A From lot B feed feed Dimethyl 9-octadecenedioate96.9 97.6

Example 25

Time of trishydroxymethyl phosphine (THMP) treatment and watertreatment, as well as type of water, were varied to study the effects onruthenium removal from a natural oil/metathesis catalyst solution.

In the experiments described, THMP was supplied from a stock solution bythe following method: 10.20 g of 75 wt % tetrakishydroxymethylphosphonium sulfate in water (Bricorr 75, Rhodia) was diluted with 37.69deionized water (Type II) under an nitrogen-inerted atmosphere 4.02 g of50 wt % sodium hydroxide (Aldrich) was then added to the dilutedsolution, followed by the addition of 4.08 g of 75 wttetrakishydroxymethyl phosphonium sulfate to the mixture, to adjust thepH to 8. The pH of the solution was measured using a pH probe. Thesolution was transferred to a plastic container and stored until use.The molar concentration of THMP in the solution was based on the totalamount of the limiting reagent sodium hydroxide (1 mole oftrishydroxymethyl phosphine=1 mole of sodium hydroxide in excesstetraki. In a 500 mL kettle flask (4 inch inner diameter), equipped withan overhead stirrer (4-pitch blades, 45°, 2 inch diameter), overheadcondenser (set at 5° C.), and baffles, a water stream containingextracted ruthenium and trishydroxymethyl phosphine (derived fromtetrakis hydroxymethyl phosphonium sulfate) was generated by thefollowing procedure:shydroxymethyl phosphonium sulfate).

In a 500 mL kettle flask (4 inch inner diameter), equipped with anoverhead stirrer (4-pitch blades, 45°, 2 inch diameter), overheadcondenser (set at 5° C.), and baffles, a water stream containingextracted ruthenium and trishydroxymethyl phosphine (derived fromtetrakis hydroxymethyl phosphonium sulfate) was generated by thefollowing procedure: 1-octene (Aldrich, 98%) was reacted with palm oil(Wilmar, refined, bleached, deodorized, pretreated at 200° C. for 2hours batch under nitrogen sparging) at a 1.5:1 molar double bond ratioof 1-octene: palm oil in the presence of 800 ppmw catalyst (C827,Materia, based on mass of oil), 60 minute batch contact time, 60° C.reaction temperature, atmospheric pressure, and under anitrogen-blanketed headspace. After generating the metathesized mixture,the mixture was heated to 90° C. and 19:1 molar equivalents oftrishydroxymethyl phosphine to catalyst (target) was added to themetathesized mixture. The metathesized mixture containingtrishydroxymethyl phosphine was stirred for 60 minutes batch. Then,deionized water (Type II) was added to the metathesized mixture at 1 gof water to 5 g of metathesized oil and stirred for 1 hour, batch at 72to 90° C. After 1 hour of water mixing, the mixture was allowed togravity settle for 1 hour while heating at 90° C. The bottom layer wasremoved from the mixture and stored. This bottom layer was assumed tosimulate a 20:1 recycle ratio of water in a continuous extractionprocess (based on a typical 40 ppmw catalyst concentration, based onmass of oil), and referred to as “Simulated Recycled Water Stream”herein.

Additional metathesized mixtures of oil were generated by reacting1-octene with palm oil (1.5:1 molar double bond ratio of 1-octene: palmoil) in the presence of 40 ppmw catalyst (based on mass of oil), 60minute batch contact time, 60° C. reaction temperature, atmosphericpressure, and under a nitrogen-blanketed headspace. A sample was removedafter 60 minutes to analyze for ruthenium concentration. Samplesgenerated from the method described are referred to as “Before THMPTreatment” herein.

After generating the additional metathesized mixture, the mixture washeated to 90° C., and 19:1 molar equivalents of trishydroxymethylphosphine to catalyst (target) was added to the metathesized mixture.The metathesized mixture containing trishydroxymethyl phosphine wasstirred for 60 minutes batch. Samples generated from the methoddescribed are referred to as “After THMP Treatment” herein.

Then, the simulated recycled water was added to the metathesized mixtureat 1 g of water to 5 g of metathesized oil and stirred for various times(15 minutes, 30 minutes, 60 minutes) batch at 72 to 90° C. After watermixing, the mixture was allowed to gravity settle for 1 hour at 90° C.The top layer and bottom layers were sampled for ruthenium concentrationand the top layer was sampled for isomerization testing. Samplesgenerated from the method described are referred to as “After WaterExtraction” herein.

Ruthenium analysis was performed using ICP-MS at STAT AnalysisCorporation, Chicago, Ill. Ruthenium efficiency (%), assuming mass isconserved, is defined by the following equation:

${{Ruthenium}\mspace{14mu}{Removal}\mspace{14mu}{Efficiency}\mspace{11mu}(\%)} = {100\frac{C_{{Ru}\mspace{14mu}{Before}\mspace{14mu}{Extraction}} - C_{{Ru}\mspace{14mu}{After}\mspace{14mu}{Extraction}}}{C_{{Ru}\mspace{14mu}{Before}\mspace{14mu}{Extraction}}}\mspace{14mu}\#}$

Isomerization tests were performed on the samples to determine theeffectiveness of the trishydroxymethyl phosphine reaction with theruthenium-containing catalyst. The isomerization test included heatingthe sample to 250° C. for 1 hour under an open-system nitrogenheadspace, maintained at 1 psig.

Standard sample analysis was performed on the isomerized samples. About6 drops (˜100-200 mg) of the sample were transferred to a 20 mLborosilicate scintillation vial. 1 mL of 1 mass % sodium methoxide inmethanol (Aldrich) was added to the vial using an autopipette. The vialwas sealed and was heated to 60 C while shaken at 240 rpm for at least40 minutes until one liquid phase was visually observed. 5 mL ofsaturated brine solution was added to the vial using an autopipette. 5mL of ethyl acetate was then added to the vial using an autopipette. Themixture was further shaken and allowed to settle into two distinctphases. Approximately 1.5-2 mL of the top layer (ethyl acetate) wastransferred to a 2 mL gas chromatography vial.

The vial was analyzed for 9-decenoic acid ester isomerization using anAgilent 7890 gas chromatograph, equipped with a split/splitllessinjection port, an RTX-65TG column (Restek 17008, 30 m length×0.25 mminner diameter×0.1 mm film thickness), quadrupole mass spectrometerdetector. Helium was used as the carrier gas.

The 9-decenoic acid ester and isomers were quantified using ionextraction of the ester fragments with the MS Chem software; theintegrated areas were assumed to be proportional to the relative massconcentration of the esters.

The percent isomerization was defined by the following equation:

${{Isomerization}\mspace{14mu}(\%)} = {100\frac{A_{{Isomer}\mspace{11mu} 1} + A_{{Isomer}\mspace{11mu} 2} + A_{{Isomer}\mspace{11mu} 3}}{A_{{Isomer}\mspace{11mu} 1} + A_{{Isomer}\mspace{11mu} 2} + A_{{Isomer}\mspace{11mu} 3} + A_{9 - {{Decenoic}\mspace{14mu}{Acid}\mspace{14mu}{Ester}}}}{\#\#}}$where A_(Isomer 1) is the integrated area of isomer 1 of 9-decenoic acidester, A_(Isomer 2) is the integrated area of isomer 2 of 9-decenoicacid ester, A_(Isomer 3) is the integrated area of isomer 3 of9-decenoic acid ester, A_(9-Decenoic Acid Ester) is the integrated areaof 9-decenoic acid ester. Isomer 1 and 2 are the cis- andtrans-8-decenoic acid methyl esters. Isomer 3 is a 7-decenoic acidmethyl ester. Other isomers can form, but are not chromatographicallyresolved from the peaks observed.

Testing was performed within 24 hours of sampling from reactor vessel.For most cases, the testing was within an hour of sampling. Sampleanalysis was run in duplicate, and an average of two runs is reported.For reference, the result of the isomerization test on a sample nottreated with THMP was typically 20-40% isomerization (average of twosamples) at the catalyst loadings studied.

TABLE 23 Water Ru content Ru removal Water Type Process Conditions Isom% (ppmw) (ppmw) eff (%) Type II DI 60 min THMP treatment, Before THMPtreatment 44.41 93 3.8 80 60 min water extraction, and After THMPtreatment 0.08 88 — 60 min settling After water extraction 0.18 15240.75 Simulated 60 min THMP treatment, Before THMP treatment 31.10 51 3.447 recycled, 20 60 min water extraction, and After THMP treatment 0.6051 — recycles, ~360 60 min settling After water extraction 0.69 1162 1.8ppmw Ru Simulated 60 min THMP treatment, Before THMP treatment 34.70 505 48 recycled, 20 30 min Water Extraction, and After THMP treatment 0.0657 — recycles, ~360 60 min settling After water extraction 0.28 1657 2.6ppmw Ru Simulated 60 min THMP treatment, Before THMP treatment 43.25 289.3 63 recycled, 20 15 min water extraction, and After THMP treatment1.06 37 — recycles, ~360 60 min settling After water extraction 0.211733 3.4 ppmw Ru Simulated 0 min THMP treatment, Before THMP treatment31.65 43 6.2 42 recycled, 20 60 min water extraction, and — — — —recycles, ~360 60 min settling After water extraction 0.57 1750 3.6 ppmwRu Simulated 15 min THMP treatment, Before THMP treatment 33.5 125.1 3.546 recycled, 20 15 min water extraction, and After THMP treatment 0.501854 — recycles, ~320 60 min settling After water extraction 0.31 9741.9 ppmw Ru

Example 26 Isomerization of 9-DAME (50 g) with Nafion SAC-13

A 250 mL 2-neck rbf was fitted with a magnetic stir bar, thermocouple,and septum. The flask was charged with 9-DAME (50 g) and Nafion SAC-13(2.5 g). The mixture was stirred at 60° C. for 18 hours, then heated to120° C. for 6 hours. The mixture was filtered to yield 46 g of a paleyellow liquid. The isomerized product was analyzed by GC and GC-MS. Todetermine the amount of isomerization, the sample was modified bydimethyl disulfide treatment, and run through the GC-MS.

Example 27 Isomerization of 9-DAME and 9-DDAME (10 g) with Nafion SAC-13

Various samples were tested in a 20 mL septa-capped scintillation vialfitted with a stir bar and vent needle. In each test, the vial wascharged with 10 g 9-DAME or 9-DDAME and between 0-10 wt % Nafion SAC-13.The vials were placed in an aluminum heating block and heated to 90° C.or 120° C. for 24 hrs. Samples were taken at 3, 6, and 24 hours for GCanalysis, and GCMS analysis after DMDS treatment. FIG. 3 compares theproduct distribution after a 24 hour isomerization reaction of 9-DAME byvarying the amount of isomerization catalyst (3 wt % versus 5 wt %).FIG. 4 compares the product distribution for a 9-DAME isomerizationreaction with 5 wt % Nafion SAC-13 loading by varying the reaction time(i.e., comparing the sample results at 6 hr and 24 hr). FIG. 5 comparesthe product distribution for a 9-DDAME isomerization reaction with 5 wt% Nafion SAC-13 loading by varying the reaction time (i.e., comparingthe sample results at 6 hr and 24 hr).

Based on these experiments, it was observed that increased temperature,increased Nafion concentration, and increased time all increased theextent of isomerization. It was also determined that under certainisomerization conditions, increased amounts of byproducts could beformed such as oligomers and γ-lactone (formed by ring closing of 4-DAMEor 4-DDAME).

Example 28 Isomerization of 9-DAME (1.2 kg) with Nafion SAC-13

1.2 kg 9-DAME and 24 g Nafion SAC-13 was added to a 2 L 3-neck roundbottom flask fitted with a condenser, a thermocouple, and a nitrogeninlet, and placed in a heating mantle. The flask was heated to 120° C.for 17 hours over 3 days, cooling overnight each time. The isomerizedsample was then flash distilled into a 2 L round bottom flask leavingbehind the oligomers, lactones, and Nafion in the pot bottoms.Yield=0.995 kg. The distilled isomerized 9-DAME can be characterized bydimethyl disulfide treatment. The distribution of isomers is displayedin FIG. 6.

Example 29 Isomerization of 9-DDAME (1.25 kg) with Nafion SAC-13

1.25 kg 9-DAME was isomerized over 2 wt % Nafion SAC-13 at 120° C. for21 hours. The isomerized sample was then flash distilled to separate thex-DDAME from the oligomers, lactones, and Nafion in the pot bottoms.Yield=1.02 kg of x-DDAME. The distribution of isomers is displayed inFIG. 7.

Example 30

In this example, t-9-ODDAME from Example 24 was isomerized to acomposition containing mono-unsaturated C18 diesters with double bondposition ranging from 3 to 9. Thus, t-9-ODDAME (1.6 Kg, having aperoxide value of 33 meq/Kg) was charged to a 3 L round bottom flaskfitted with a reflux condenser chilled to −5° C. The flask was heated to200° C. for 2 hours with a constant nitrogen purge through the liquid.After heating, the peroxide value was found to be 1.2 meq/kg. Analysisof the sample by GC/FID and GC/MS failed to reveal a significant changein composition in terms of GC peaks present, relative area counts, ormass spectrum (at 70 ev) of each peak. Surprisingly, the melting pointof the new composition (17.6° C.) was substantially reduced from that oftrans-9-ODDAME (30.6° C.) or cis,trans-9-ODDAME (26.7° C.). To determinedouble bond position, the composition was reacted with dimethyldisulfideand further analyzed by GC/MS according to the method of Francis, G. W.“Alkylthiolation for the determination of double-bond position inunsaturated fatty acid esters” (Chem. Phys. Lipids, 29, 369-374, 1981).By this method, each mono-unsaturated C18 diester is expected togenerate two fragments whose mass corresponds to the location of thedouble bond in the diester. Additionally, loss of the elements ofmethanol generates another set of fragments. The table below listsindicative fragments expected for all un-branched mono-unsaturated C18diesters and which were observed in analysis of the new composition.

TABLE 24 Fragment mass - dimethyldisulfide adducts of unbranchedmonounsaturated C18 diesters Fragment 1 Fragment 2 Present in (loss ofCH₄O) (loss of CH₄O) composition? 9-ODDAME 217 (185) 217 (185) Yes8-ODDAME 203 (171) 231 (199) Yes 7-ODDAME 189 (157) 245 (213) Yes6-ODDAME 175 (143) 259 (227) Yes 5-ODDAME 161 (129) 273 (241) Yes4-ODDAME 147 (115) 287 (255) Yes 3-ODDAME 133 (101) 301 (269) Yes2-ODDAME 119 (87)  315 (283) No

Example 31

In this example, the isomerized composition from Example 30 was reactedin the presence C-827 metathesis catalyst to give a distribution ofmono-unsaturated diesters of carbon-chain length from 10 to 28. Thus,C-827 (21.10 mg) was placed in a 2 mL volumetric flask. The flask wasthen capped with a rubber septum and purged with nitrogen. Toluene wasadded to the 2.00 mL mark thus making a 0.01 mg/μL solution of catalyst.A portion of the isomerized composition was placed in a 20 mL septum topvial with a rare earth stir bar. The vials were placed in an eight-cellaluminum block on top of a heater/stirrer. The aluminum block was heatedto 60° C. and the isomerized composition was degassed by spargingnitrogen through the melt for 5 min. The temperature was raised to 70°C. and metathesis catalyst was added (time=0).

Table 25 below depicts the catalyst charge and amount of isomerizedcomposition for 4 tests.

TABLE 25 Catalyst Test # Charge (ppm) 9-ODDAME (g) 1 20.1 10.02 2 39.810.11 3 78.6 10.23 4 120.1 10.04

Table 26 below depicts the mole fraction dibasic ester by carbon numberafter 3 three hours for the four examples.

TABLE 26 mole fraction - monounsaturated dibasic ester by carbon numberC # Test #1 Test #2 Test #3 Test #4 10 0.0000 0.0000 0.0014 0.0029 110.0000 0.0000 0.0046 0.0079 12 0.0000 0.0006 0.0095 0.0168 13 0.00040.0025 0.0186 0.0317 14 0.0011 0.0048 0.0312 0.0523 15 0.0019 0.00740.0467 0.0769 16 0.0027 0.0101 0.0622 0.1009 17 0.0196 0.0272 0.08090.1200 18 0.9580 0.8991 0.4698 0.1517 19 0.0069 0.0159 0.0786 0.1232 200.0032 0.0113 0.0662 0.1052 21 0.0027 0.0088 0.0517 0.0820 22 0.00180.0059 0.0358 0.0571 23 0.0009 0.0034 0.0219 0.0356 24 0.0004 0.00180.0120 0.0197 25 0.0002 0.0008 0.0057 0.0096 26 0.0000 0.0003 0.00230.0040 27 0.0000 0.0000 0.0008 0.0014 28 0.0000 0.0000 0.0002 0.0004

Example 32 Comparative Example

Batch Hydrogenation of trans-9-ODDAME in 600 mL Parr reactor system.Pricat 9910 is a hydrogenation catalyst consisting of finely dispersedNickel on a silica support and suspended in hardened triglyceride.Toluene (5.87 g, Sigma Aldrich anhydrous) was added to Johnson MattheyPricat 9910 catalyst (1.13 g) in a 20 mL vial. The mixture was brieflystirred and then allowed to settle overnight at room temperature(approx. 20-25° C.). The toluene supernatant layer was removed bypipette.

Trans-9-octadecenedioic acid (t-9-ODDAME, 242.04 g) was pre-melted in50° C. oven in a clean, dry stainless steel 600 mL Parr reactor vesselbottom. The solid Nickel catalyst described in Example 24 above wasadded to the reactor vessel using the isomerized composition fromExample 30 9-ODDAMe (8.00 g) as a rinse. The Parr reactor was sealed andthe system was leak checked with 500 psig nitrogen for 15 minutes. Thereactor is equipped with a heating mantle, dip tube, sampling valve, gasentrainment stirrer, internal cooling loop, thermocouple, and headspacegas release valve. The high pressure nitrogen was vented from thereactor headspace and the system was purged with low pressure nitrogen,0.3 LPM, thru the dip tube for 15 minutes. Positive nitrogen pressure,<20 psig, was left in the reactor headspace before the system wassealed. The reactor system was then purged with hydrogen thru the diptube for 15 minutes. 50 psig of hydrogen was charged into the reactorheadspace and the system was sealed. The reactor contents were slowlyheated to 150° C., the stirrer speed was increased to 915 rpm, and theheadspace pressure was increased to 150 psig over one hour. Hydrogenuptake was observed and replacement hydrogen was added thru the dip tubeas needed to maintain a reactor headspace pressure of approximately 150psig. After one hour, the stirrer speed was increased to 970 rpm ashydrogen uptake slowed. The hydrogenation reaction continued for 2 morehours, at the point when no noticeable hydrogen uptake was observedwithin an hour. The reaction was then allowed to cool to 75° C., and thereactor headspace was vented. The reactor contents were purged with lowpressure nitrogen, 0.3 LPM, thru the dip tube for 15 minutes. Thereactor was disassembled. After removing a 3.08 g retain sample, thewarm (˜80 C) product was filtered through 9.40 g of diatomaceous earthto give 227.21 g of filtrate. The filter cake (diatomaceous earth,catalyst, and product) weighed 22.53 g.

Example 33

Batch Hydrogenation of the isomerized composition in 600 mL Parr reactorsystem. Pricat 9910 is a hydrogenation catalyst consisting of finelydispersed Nickel on a silica support and suspended in hardenedtriglyceride. Toluene (5.57 g, Sigma Aldrich anhydrous) was added toJohnson Matthey Pricat 9910 catalyst (1.13 g) in a 20 mL vial. Themixture was briefly stirred and then allowed to settle overnight at roomtemperature (approx. 20-25° C.). The toluene supernatant layer wasremoved by pipette.

The isomerized composition (250.04 g) and the solid Nickel catalystdescribed in Example 30 above were added to a clean, dry stainless steel600 mL Parr reactor vessel bottom. The Parr reactor was sealed and thesystem was leak checked with 500 psig nitrogen for 15 minutes. Thereactor is equipped with a heating mantle, dip tube, sampling valve, gasentrainment stirrer, internal cooling loop, thermocouple, and headspacegas release valve. The high pressure nitrogen was vented from thereactor headspace and the system was purged with low pressure nitrogen,0.3 LPM, thru the dip tube for 15 minutes. Positive nitrogen pressure,<20 psig, was left in the reactor headspace before the system wassealed. The reactor system was then purged with hydrogen thru the diptube for 15 minutes. 50 psig of hydrogen was charged into the reactorheadspace and the system was sealed. The reactor contents were slowlyheated to 150° C., the stirrer speed was increased to 915 rpm, and theheadspace pressure was increased to 150 psig over one hour. Hydrogenuptake was observed and replacement hydrogen was added thru the dip tubeas needed to maintain a reactor headspace pressure of approximately 150psig. The hydrogenation reaction continued for 3.5 hours, at the pointwhen no noticeable hydrogen uptake was observed within an hour. Thereaction was then allowed to cool to 80° C., and the reactor headspacewas vented. The reactor contents were purged with low pressure nitrogen,0.3 LPM, thru the dip tube for 15 minutes. The reactor was disassembled.After removing a 12.03 g retain sample, the warm (˜80 C) product wasfiltered through 10 g of diatomaceous earth to give 221.59 g offiltrate. The filter cake (diatomaceous earth, catalyst, and product)weighed 18.58 g.

Table 27 below shows the composition of hydrogenation products oft-9-ODDAME and the isomerized composition.

TABLE 27 Product Composition (wt %) from Hydrogenation Experiments FromFrom isomerized t-9-ODDAME composition decanoic acid, methyl ester 0.010.02 undecanoic acid, methyl ester 0.05 0.06 dodecanoic acid, methylester ND Trace pentadecanoic acid, methyl ester 0.01 0.01 hexadecanoicacid, methyl ester 0.28 0.23 heptadecanoic acid, methyl ester 0.01 0.01octadecanoic acid, methyl ester 0.05 0.04 nonadecanoic acid, methylester 0.03 0.03 hexadecanedioic acid, methyl ester 0.01 0.02heptadecanoic acid, methyl ester 1.59 1.67 octadecanedioic acid,dimethyl ester 97.2  97.5  nonadecanedioic acid, dimethyl ester 0.060.24 eicosanedioic acid, dimethyl ester 0.06 0.02

Example 34 Solubility of Saponified x-DDA and 9-DDA Salts, RoomTemperature

Isomerization of esters of 9-DDA were performed, giving x-9DDA estersusing procedures such as those described in Example 29 above. The x-9DDAand 9-DDA esters were also saponified under typical saponificationconditions (e.g., with KOH and water). The saponified esters (x-DDA saltor 9-DDA salt) were added incrementally to room temperature water (0.88mL, approx. 20-25° C.) in a scintillation vial. The solution was stirredaggressively for a minimum of ten minutes; if the salt dissolved, morewas added to the solution. Once the salt no longer dissolved, theendpoint for the solubility test had been reached. The results of thesolubility tests are shown below in Table 28.

TABLE 28 Minimum Solubility (the solubility of Maximum Solubility thesalt in water (the solubility of is greater than the salt in water Avg.Solubility or equal to the is less than the [(Min + Compoundconcentration given) concentration given) Max)/2] 9-DDA 0.50 g salt/0.61 g salt/ 0.63 +/− 0.06 Salt 0.88 g H₂O = 0.88 g H₂O = 0.57 g salt/gH₂O 0.69 g salt/g H₂O x-DDA 0.61 g salt/ 0.71 g salt/ 0.75 +/− 0.06 Salt0.88 g H₂O = 0.88 g H₂O = 0.69 g salt/g H₂O 0.81 g salt/g H₂O

Example 35 Solubility of Saponified x-DDA and 9-DDA Salts, 0° C.

Isomerization of esters of 9-DDA were performed, giving x-9DDA estersusing procedures such as those described in Example 29 above. The x-9DDAand 9-DDA esters were also saponified under typical saponificationconditions (e.g., with KOH and water). The saponified esters (x-DDA saltor 9-DDA salt) were added incrementally to water (2 mL) in ascintillation vial. The solution was stirred aggressively for a minimumof ten minutes in an ice bath (0° C.); if the salt dissolved, more wasadded to the solution. Once the salt no longer dissolved, the endpointfor the solubility test had been reached. The results of the solubilitytests are shown below in Table 29.

TABLE 29 Minimum Solubility (the solubility of Maximum Solubility thesalt in water (the solubility of is greater than the salt in waterSolubility or equal to the is less than the [(Min + Compoundconcentration given) concentration given) Max)/2] 9-DDA 1.2134 g salt/1.2656 g salt/ 0.62 +/− 0.01 Salt 2.0099 g H₂O = 2.0099 g H₂O = 0.604 gsalt/g H₂O 0.630 g salt/g H₂O x-DDA 1.3148 g salt/ 1.3679 g salt/ 0.67+/− 0.01 Salt 2.0072 g H₂O = 2.0072 g H₂O = 0.655 g salt/g H₂O 0.681 gsalt/g H₂O

Unless otherwise described, the aforementioned examples utilized thefollowing analytical methods described below:

Volatile products were analyzed by gas chromatography and flameionization detector (FID). Alkene analyses were performed using anAgilent 6890 instrument and the following conditions:

-   -   Column: Restek Rtx-5, 30m×0.25 mm (ID)×0.25 μm film thickness    -   Injector temperature: 250° C.    -   Detector temperature: 280° C.    -   Oven temperature: 35° C. starting temperature, 4 minute hold        time, ramp rate 12° C./min to 260° C., 8 minute hold time    -   Carrier gas: Helium    -   Mean gas velocity: 31.3±3.5% cm/sec (calculated)    -   Split ratio: ˜50:1

The products were characterized by comparing peaks with known standards,in conjunction with supporting data from mass spectrum analysis(GCMS-Agilent 5973N). GCMS analysis was accomplished with a secondRtx-5, 30m×0.25 mm (ID)×0.25 μm film thickness GC column, using the samemethod as above.

Alkane analyses were performed using an Agilent 6850 instrument and thefollowing conditions:

-   -   Column: Restek Rtx-65, 30 m×0.32 mm (ID)×0.1 μm film thickness    -   Injector temperature: 250° C.    -   Detector temperature: 350° C.    -   Oven temperature: 55° C. starting temperature, 5 minute hold        time, ramp rate 20° C./min to 350° C., 10 minute hold time    -   Carrier gas: Hydrogen    -   Flow rate: 1.0 mL/min    -   Split ratio: 40:1

The products were characterized by comparing peaks with known standards.Fatty acid methyl ester (FAME) analyses were performed using an Agilent6850 instrument and the following conditions:

-   -   Column: J&W Scientific, DB-Wax, 30 m×0.32 mm (ID)×0.5 μm film        thickness    -   Injector temperature: 250° C.    -   Detector temperature: 300° C.    -   Oven temperature: 70° C. starting temperature, 1 minute hold        time, ramp rate 20° C./min to 180° C., ramp rate 3° C./min to        220° C., 10 minute hold time    -   Carrier gas: Hydrogen    -   Flow rate: 1.0 mL/min        The examples above collectively demonstrate the major steps        described in the process schemes, showing the production of        olefins, paraffins, metathesized triglycerides, unsaturated        fatty acid esters and acids, and diacid compounds from natural        oils that are useful as chemicals, solvents and fuels blending        stocks.

What is claimed is:
 1. A method of making an isomerized ester, comprising: providing a C4-C22 unsaturated fatty acid ester; and isomerizing the C4-C22 unsaturated fatty acid ester in the presence of heat or an isomerization catalyst to form an isomerized acid ester; wherein the isomerization catalyst is (PCy₃)₂(Cl)(H)Ru(CO) or a sulfonated tetrafluoroethylene polymer; and wherein the melting point of the isomerized acid ester is reduced by at least 10° C. in comparison to the C4-C22 unsaturated fatty acid ester.
 2. The method of claim 1, wherein the unsaturated fatty acid ester is derived from transesterifying a natural oil feedstock in the presence of an alcohol to form the unsaturated fatty acid ester.
 3. The method of claim 1, wherein the unsaturated fatty acid ester is selected from the group consisting of: pentenoic acid esters, hexenoic acid esters, heptenoic acid esters, octenoic acid esters, nonenoic acid esters, decenoic acid esters, undecenoic acid esters, dodecenoic acid esters, tridecenoic acid esters, tetradecenoic acid esters, pentadecenoic acid esters, hexadecenoic acid esters, heptadecenoic acid esters, octadecenoic acid esters, and mixtures thereof.
 4. The method of claim 1, wherein the solubility of the isomerized acid ester at ambient temperature is at least 10% higher in comparison to the solubility of the C4-C22 unsaturated fatty acid ester in the same solvent.
 5. The method of claim 1, wherein the isomerizing step is conducted by heating a reactor containing unsaturated fatty acid ester to a temperature greater than 100° C.
 6. The method of claim 1, wherein unsaturated fatty acid ester comprises a terminal olefin ester having the following structure:

wherein X is a C₃-C₁₈ saturated or unsaturated alkyl chain, and R is an alkyl group.
 7. The method of claim 6, wherein R is methyl.
 8. The method of claim 6, further comprising, prior to the isomerizing step: providing an internal olefin; and reacting the terminal olefin ester with the internal olefin in the presence of a metathesis catalyst to form a dibasic ester, wherein, in the subsequent isomerizing step, forming a isomerized dibasic ester.
 9. The method of claim 8, further comprising hydrogenating the isomerized dibasic ester.
 10. The method of claim 8, further comprising reacting the isomerized dibasic ester with itself or a low-molecular-weight olefin in the presence of metathesis catalyst to form a metathesized dibasic ester.
 11. The method of claim 8, wherein the terminal olefin ester is selected from the group consisting of: 4-pentenoic acid ester, 5-hexenoic acid ester, 6-heptenoic acid ester, 7-octenoic acid ester, 8-nonenoic acid ester, 9-decenoic acid ester, 10-undecenoic acid ester, 11-dodecenoic acid ester, 12-tridecenoic acid ester, 13-tetradecenoic acid ester, 14-pentadecenoic acid ester, 15-hexadecenoic acid ester, 16-heptadecenoic acid ester, 17-octadecenoic acid ester, and mixtures thereof.
 12. The method of claim 8, wherein the terminal olefin is 9-decenoic acid ester.
 13. The method of claim 8, wherein the internal olefin ester is selected from the group consisting of: pentenoic acid esters, hexenoic acid esters, heptenoic acid esters, octenoic acid esters, nonenoic acid esters, decenoic acid esters, undecenoic acid esters, dodecenoic acid esters, tridecenoic acid esters, tetradecenoic acid esters, pentadecenoic acid esters, hexadecenoic acid esters, heptadecenoic acid esters, octadecenoic acid esters, and mixtures thereof.
 14. The method of claim 8, wherein the internal olefin is 9-dodecenoic acid ester.
 15. The method of claim 8, further comprising hydrolyzing the isomerized dibasic ester to form an isomerized dibasic acid. 